CN102276644A

CN102276644A - Transition metal-carbide and nitride containing catalysts, their preparation and use as oxidation and dehydrogenation catalysts

Info

Publication number: CN102276644A
Application number: CN2011101131923A
Authority: CN
Inventors: F·刘; J·阿兰塞特; R·麦卡尔; D·A·莫根斯特恩; K-T·旺
Original assignee: Monsanto Co
Current assignee: Monsanto Co
Priority date: 2003-08-14
Filing date: 2004-08-16
Publication date: 2011-12-14
Anticipated expiration: 2024-08-16
Also published as: WO2005016519A1; MXPA06001800A; BRPI0413586A; US8697904B2; EP2460586A2; EP1684900B1; US20050176989A1; CA2534819A1; AU2004264436B2; US20110301381A1; US20140235432A1; US7932419B2; CN1867404A; AR083305A2; AU2004264436A1; AR045271A1; EP1684900A1; ES2407031T3; CN102276644B; CN1867404B

Abstract

Catalysts including carbon supports having formed thereon compositions which comprise a transition metal carbide, nitride or carbide-nitride are prepared. The catalysts are useful for catalytic oxidation and dehydrogenation reactions, including the preparation of secondary amines by the catalytic oxidation of tertiary amines and the preparation of carboxylic acids by the catalytic dehydrogenation of alcohols.

Description

Contain the catalyzer of transition metal-carbide and nitride, their preparation method and as the purposes of oxidation and dehydrogenation catalyst

The present invention is dividing an application of patent application No.200480030049.6, the applying date of this patent application is on August 16th, 2004, and invention and created name is " contain the catalyzer of transition metal-carbide and nitride, their preparation method and as the purposes of oxidation and dehydrogenation catalyst ".

Invention field

The present invention relates to the field of heterogeneous catalysis, relate more specifically to comprise the catalyzer of carbon support, on carbon support, formed the composition that contains with nitrogen and/or carbon bonded transition metal.The invention further relates to the field of catalyzed oxidation and dehydrogenation reaction, prepare the method for secondary amine and prepare the method for carboxylic acid by the catalytic dehydrogenation of alcohol comprising catalyzed oxidation by tertiary amine.

Background of invention

Comprise the evaluation of the suitability of carbide and nitride material for the research work of the selective material of finding to be used for the reaction of catalysis all kinds.Generally, carbide and nitride material have been considered to the possible alternatives that can use for various types of catalysis, because they demonstrate " metal shape " performance (for example high fusing point, hardness and intensity).Levy﹠amp; Boudart has reported that carbide and nitride material demonstrate and the similar catalytic performance of the catalytic performance of precious metal.Referring to Platinum-Like Behavior of Tungsten Carbide in Surface Catalysis (Science, 181 (1973), 547-549).

Carbide that supports and nitride generally have been described and have been reported to and be suitable in various types of reactions.People such as Slaugh have described by ten dichloros, six molybdenums being impregnated into porous and have contained aluminium (Al for example ₂O ₃), prepare the molybdenum carbide composition that supports on the carrier of siliceous or carbon containing (for example gac), then it is heated in the carbonization atmosphere under about 650 ℃-750 ℃ temperature.Referring to US patent No.4,325,842.

People such as Leclercq have reported and have used the catalystic reforming method that carries out based on the catalyzer that is supported on tungsten on aluminum oxide and the gac and molybdenum carbide.Referring to U.S. Patent No. 4,522,708.These catalyzer are following to be made: use ammonium molybdate and ammonium tungstate solution Immesion active carbon in succession, evaporate to dryness in air is calcined in nitrogen atmosphere then, allows then formed tungsten and molybdenum oxide reduce in nitrogen atmosphere in calcination process.These compounds heat in nitrogen atmosphere then, allow the reaction of active phase compound and carbon support to produce the mixed carbide of tungsten and molybdenum.

People such as Sherif have reported by will being calcined the formed catalyzer that contains carbon-supported group vib metal (for example Cr, Mo, W) carbide with the impregnated carbon support of water-soluble precursor (for example gac and acid-washed active carbon) of metallic carbide.Referring to international publication No.WO 95/32150.

Oyama has reported the alloy that the space is arranged, and it forms by producing the compounds with metallic character in the lattice that carbon, nitrogen and oxygen is incorporated into transition metal morning.Preparation and catalytic performance (Preparation and Catalytic Properties of Transition Metal Carbides and Nitrides) (Catalysis Today, 15,179-200,1992) referring to transition metal carbide and nitride.

People such as Iwai have reported that by the carbide of IV, V and VI family metal and the carbonitride that nitride is formed it is calcined preparation by the precursor that will be obtained by the halid reaction of polyphenol and ammonia and IV, V or VI family metal.This precursor also can be by polyphenol and IV, V or VI family metal halid reaction product and ammonia react and obtain.Referring to US patent No.4,333,916.

People such as Faubert have reported and have prepared the method that contains iron carbide particulate iron-containing catalyst, and this particle is to utilize hydrogen reduction and the pyrolysis in the presence of acetonitrile, will be activated by the precursor that the ironic hydroxide that is adsorbed on the carbon black is formed to prepare.Referring to Activation and characterization of Fe-based catalysts for the reduction of oxygen in polymer electrolyte fuel cells (Electrochimica Acta, Vol.43, Nos.14-15, pp.1969-1984,1998).

People such as Cote have reported base metal type Preparation of catalysts method, it prepares by the pyrolysis of the transition metal hydroxide on carbon black (for example oxyhydroxide of vanadium, chromium, iron, cobalt), is included in reduction and the heating in the presence of acetonitrile under the hydrogen existence.Referring to Non-noble metal-based catalysts for the reduction of oxygen in polymer electrolyte fuel cells (Journal of New Materials for Electrochemical Systems, 1,7-16,1998).

The catalyzer that contains carbide or nitride is favourable in some cases, owing to not containing expensive precious metal.Wherein not needing to have the active catalyst of precious metal is that favourable a kind of this type of reaction is to produce the reaction of secondary amine (for example N-((phosphonomethyl)) glycine) with tertiary amine (for example N-((phosphonomethyl)) iminodiethanoic acid) oxidation.N-((phosphonomethyl)) glycine (being known as " glyphosate " in agrochemicals industry) is described in the US patent No.3 of Franz, in 799,758.N-((phosphonomethyl)) glycine and its salt can make things convenient for as the post-emergence herbicide in the water-based preparaton to be used.It is the very effective and industrial important broad-spectrum herbicide that can be used for killing or control the growth of various plant, and these plants comprise germinating seed, seedling, ripe and the wooden and herbaceous plant that grows up to, and waterplant.

The whole bag of tricks of producing N-((phosphonomethyl)) glycine is known in the prior art.Franz (US patent No.3; 950,402) instructed N-((phosphonomethyl)) glycine can be by preparing by N-((phosphonomethyl)) iminodiethanoic acid (being sometimes referred to as " PMIDA ") liquid-phase oxidation cracking comprising in the presence of the catalyzer that is deposited on the precious metal on the activated carbon carrier surface with oxygen:

Also can form other by product, formic acid for example, it is formed by the oxidation of formaldehyde by product; And aminomethylphosphonic acid (" AMPA "), it is that oxidation by N-((phosphonomethyl)) glycine forms.Though described Franz method is produced N-((phosphonomethyl)) glycine with acceptable yields and purity; but expensive precious metal is lost in the reaction soln (promptly relatively largely; " lixiviate "); because under the oxidizing condition of reaction, some precious metals are oxidized to the effect that more diffluent form and PMIDA and N-((phosphonomethyl)) glycine have all played the part that makes the precious metal solubilising.

In U.S. Patent No. 3,969, in 398, Hershman has instructed gac (not have precious metal) individually to be used to carry out the oxicracking of PMIDA to form N-((phosphonomethyl)) glycine.In US patent No 4,624,937, Chou further instructs: the activity by the C catalyst of Hershman instruction can improve by removed oxide compound from the surface of C catalyst before catalyzer is used for oxidizing reaction.Also referring to US patent No.4,696,772, wherein provide the independent discussion of Chou, about improving the C catalyst activity by removing oxide compound from the surface of C catalyst.Though these methods obviously do not run into the problem of precious metal lixiviate, when being used to carry out the oxicracking of N-((phosphonomethyl)) iminodiethanoic acid, they tend to produce the formaldehyde by product of bigger concentration.This formaldehyde by product is disadvantageous; because it (mainly is N-methyl-N-((phosphonomethyl)) glycine that it and N-((phosphonomethyl)) glycine reactant produce disadvantageous by product; be sometimes referred to as " NMG "), this has reduced the productive rate of N-((phosphonomethyl)) glycine.In addition, the formaldehyde by product itself is disadvantageous, because it has potential toxicity.Referring to Smith, U.S.Patent No.5,606,107.

Advise that formaldehyde is oxidized to carbonic acid gas and water simultaneously, and PMIDA is oxidized to N-((phosphonomethyl)) glycine in single reactor, therefore provides following reaction:

As above training centre suggestion, these class methods need exist carbon (it is mainly used in the oxidation of carrying out PMIDA and forms N-((phosphonomethyl)) glycine and formaldehyde) and precious metal (it is mainly used in the oxidation of carrying out formaldehyde and forms formic acid, carbonic acid gas and water).Yet the previous trial that exploitation is used for the rugged catalyst of this type of oxidising process is not entirely satisfactory.

With Franz similarly, people such as Ramon (US patent No.5,179,228) have instructed to use and have been deposited over the lip-deep precious metal of carbon support.Yet, in order to reduce the problem of lixiviate (people such as Ramon has reported the phase of loss up to 30% precious metal/weekly), people such as Ramon have instructed after oxidizing reaction is finished and have washed reaction mixture with nitrogen pressure, cause that precious metal deposits on the surface of carbon support again.According to people's such as Ramon report, nitrogen wash is brought down below 1% with precious metal losses.The precious metal losses amount that this method runs into remains unacceptable.In addition, deposit this precious metal again and can cause the long-pending loss of precious metal surface, and then reduce activity of such catalysts.

By using diverse ways, Felthouse (US patent No.4,582; 650) two kinds of catalyzer are used in instruction: (i) activated carbon; be used to carry out from PMIDA to the oxidation of N-((phosphonomethyl)) glycine and (ii) promotor, the oxidation of carrying out formaldehyde simultaneously obtains carbonic acid gas and water.Promotor is by being made up of the aluminosilicate carrier of precious metal in hole.These holes have suitable dimension to get rid of N-((phosphonomethyl)) glycine and to prevent that therefore the precious metal of promotor from being poisoned by N-((phosphonomethyl)) glycine.According to Felthouse, the use together of these two kinds of catalyzer makes PMIDA be oxidized to N-((phosphonomethyl)) glycine and makes oxidation of formaldehyde become carbonic acid gas and water simultaneously.Yet there are several shortcomings in this method: (1) is difficult to reclaim expensive precious metal for re-using from aluminosilicate carrier; (2) be difficult to design these two kinds of catalyzer so that their ratios between the two mate; (3) carbon support is not deposited on its lip-deep precious metal, tends to surpass the speed deactivation of 10%/weekly phase.

People such as Ebner are at US patent No.6,417, precious metal/the C catalyst of drastic reduction has been described in 133, it is characterised in that: when the dry sample of catalyzer, in nitrogen atmosphere under about 500 ℃ temperature after about 1 hour of the heating and before heating afterwards is exposed to oxygenant in nitrogen atmosphere, in helium-atmosphere, be heated to about 900 ℃ and from about 20 ℃, be lower than 1.2mmol/g, preferably be lower than the CO desorb of 0.5mmol/g then in about 900 ℃ of heating in the time of about 30 minutes down with the speed of about 10 ℃/per minute.This catalyzer embody in addition or in addition feature in have from the teeth outwards at least about 20: 1, preferably at least about 30: 1 the carbon atom and the ratio of Sauerstoffatom, according to catalyzer in nitrogen atmosphere about 500 ℃ down after about 1 hour of the heating and in nitrogen atmosphere after the heating catalyst exposure before oxygenant by the measured result of x-ray photoelectron spectroscopy.

US patent No.6; 417; 133 catalyzer has proved and has been used for N-((phosphonomethyl)) iminodiethanoic acid is oxidized to N-((phosphonomethyl)) glycine and be used for the highly beneficial and effective catalyzer of the further oxidation of by product formaldehyde and formic acid, and does not have precious metal excessive lixiviate problem from carbon support.Find further that also these catalyzer are effective in the operation of the continuation method of being produced N-((phosphonomethyl)) glycine by the oxidation of N-((phosphonomethyl)) iminodiethanoic acid.

At US patent No.6; 417; the carbon of 133 catalyzer and precious metal site be metastatic electron in the oxidation of N-((phosphonomethyl)) iminodiethanoic acid very effectively, and these precious metal sites are effective for this purpose in the oxidation of formaldehyde and formic acid especially.Yet; such many catalysts and reaction method are advantageously arranged: it PMIDA is oxidized to N-((phosphonomethyl)) glycine and demonstrate simultaneously desirable from formaldehyde (promptly to the oxidation of carbonic acid gas and water; the formaldehyde activity that improves) and it does not need exist (for example catalyzer of carbide-containing, nitride or carbide-nitride) of precious metal.In addition or as an alternative; such many catalysts and reaction method are arranged also advantageously: for the catalyzer of the industrial production that is used for N-((phosphonomethyl)) glycine or other secondary amine at present, they do not need expensive precious metal or them just can play a role effectively with the bullion content that reduces.

The salt of iminodiethanoic acid can be by phosphonomethyl formation PMIDA, it so that according to the oxidized formation of above narration N-((phosphonomethyl)) glycine.

Referring to the US patent No.4 of for example Gentilcore, 775,498 (disclosing the method for the salt of iminodiethanoic acid being carried out ization); People's such as Ebner US patent No.6,417,133 (disclosing the method for oxidation PMIDA).

For example the salt of nitrilotriacetic acid(NTA) is excellent sequestrant, therefore can be used as detergent builder, water-softening agent, scrubs auxiliary agent, dyeing auxiliary, paper and coating agent, scale inhibitor and prevent the reagent that soap is degenerated.Many aminocarboxylates (for example the salt of the salt of glycine, iminodiethanoic acid etc.) also can be neutralized into their respective acids, then for example as sequestrant; Be used for food mfg; With raw material as manufacturing medicine, agrochemicals and sterilant.Referring to people such as for example Franz; Glyphosate:A Unique Global Herbicide (ACS Monograph 189; 1997), pp.234-41 (disclosing glycine and iminodiacetic acid compounds) as the raw-material purposes that forms N-((phosphonomethyl)) glycine.

Be known that for a long time carboxylate salt can be by using cupric or argentiferous catalyzer with the primary alconol dehydrogenation and from this primary alconol preparation.1945, Chitwood has at first reported and has used copper bearing catalyzer (specifically copper metal or cupric oxide, the latter it is reported and be reduced into the copper metal under reaction conditions) or argentiferous catalyzer (specifically silver metal or silver suboxide, the latter it is reported and be reduced into silver metal under reaction conditions), at alkaline environment (specifically containing in the mixture of potassium hydroxide) primary alconol (monoethanolamine specifically) is carried out oxidation to form carboxylate salt (sylvite of glycine specifically).Referring to the US patent No.2 of Chitwood, 384,817.Yet Chitwood reports that copper-containing compound is disadvantageous for this reaction, because copper condenses in time, therefore causes copper-containing compound to have the time weak point of maximum catalytic activity.Chitwood reports that also Ag-containing compound has low relatively activity (silver suboxide also is in the news and condenses in time).

1988, people such as Goto reported interior (Raney) copper of use Ruan and in basic solution (aqueous solution that specifically contains the oxyhydroxide of basic metal or alkaline-earth metal) the ethanolamine compound oxidation have been formed carboxylate salt.Referring to people's such as Goto US patent No.4,782,183.People such as Goto have reported when the selectivity that monoethanolamine, diethanolamine and trolamine is had 94.8% when dehydrogenation forms glycine, iminodiethanoic acid and nitrilotriacetic acid(NTA) respectively at least.Yet copper is disadvantageous in Ruan, because copper in time and deactivation in (similar with the copper-containing compound of Chitwood) Ruan.Referring to the US patent No.5 of for example Franczyk, 292,936, table 1 (having shown that through 9 cycles the reaction times of copper was increased to 8 hours from 4 hours in Ruan).

The various progress that are used to solve the instability problem of copper containing catalyst when being used for the primary alconol dehydrogenation have been reported.Though these progress have been used at industrial more feasible copper catalyst, their result still is not entirely satisfactory.

People such as Ebner have reported a kind of method that carboxylate salt produced the primary alconol dehydrogenation by the catalyzer that is supported on the copper on the alkaline-resisting carrier (especially carbon support) that comprises of using.Referring to people's such as Ebner US patent No.5,627,125.This catalyzer also comprises the precious metal of about 0.05-10 weight % so that with the copper anchoring be distributed on the carrier.Though the Ebner catalyzer has obtained the reaction times shorter than previously disclosed copper containing catalyst, this catalyzer is relatively costly, uses precious metal that copper is anchored on the carrier owing to needs.People's such as Ebner catalyzer is usually in use passed in time and is lost activity (though the speed of deactivation usually is lower than the deactivation speed of Franczyk catalyzer).Referring to people such as for example Ebner, table 1 (showing that the reaction times was increased to 150 minutes from 103 minutes through 9 cycles) and table 2 (showing that the reaction times was increased to 155 minutes from 61 minutes through 8 cycles).For the Franczyk catalyzer, especially when being sequestrant, primary alconol or dehydrogenation product salt tend to take place this problem.

People such as Morgenstern have reported cupric or the silver-containing catalyst that comprises the metallic carrier (for example metal sponge carrier) that scribbles copper or silver by use, the method for primary alconol (for example amino alcohol such as diethanolamine) dehydrogenation being produced carboxylate salt (for example disodium of iminodiethanoic acid).Referring to people's such as Morgenstern US patent No.6,376,708.The catalyzer of being described by people such as Morgenstern may further include non-copper or the non-silver metal that is deposited on the carrier, and has deposited cupric or argentiferous catalyst activity phase thereon.People's such as Morgenstern catalyzer is the economy substitute of the copper containing catalyst known in the past, because it does not need expensive precious metal, as needed those precious metals in the catalyzer of describing people such as Ebner, meanwhile demonstrate acceptable and improved weather resistance of potentiality and activity.Yet have been found that the catalyzer of being described by people such as Morgenstern can cause producing undesirable by product (for example sarkosine), they have disadvantageous effect for those methods of wherein introducing the carboxylate salt that uses this Catalyst Production.

The copper containing catalyst of other report contains non-carbon support, as SiO ₂, Al ₂O ₃, TiO ₂, ZrO ₂Deng.(disclose by at ZrO referring to the WO 98/13140 of for example Akzo Nobel ₂On the catalyzer formed of copper).Yet these carriers tend to be worn easily under the reaction conditions of normal presence with the primary alconol dehydrogenation time, therefore more are not suitable for using than people's such as Ebner carbon support usually.Be easy to wear and tear and also tend to cause these carriers to show the filtering feature of difference.

Also reported the use in other type oxidizing reaction of cupric and silver-containing catalyst.Yet the applicant does not know any this type of disclosure of these problems relevant with cupric or silver-containing catalyst in the method that involves primary alconol dehydrogenation formation carboxylate salt.

Therefore, though for using copper containing catalyst, especially carbon-supported copper containing catalyst primary alconol to be changed into carboxylate salt reported positive progress, but still need more economical catalyzer, it should have high surface area, has high reactivity, demonstrates stability (promptly keeping its activity) in time and at utmost reduce unfavorable production of by-products.When primary alconol substrate and/or carboxylate salt product were sequestrant (for example salt of iminodiethanoic acid), this need be urgent especially.Still demand is used for alcohol dehydrogenase, is particularly useful for diethanolamine is dehydrogenated to the alternative catalysts of iminodiethanoic acid or its salt.Also still demand does not need to exist this type of catalyzer that is used for copper activity is anchored to mutually the precious metal on the carrier.Be desirable to provide this type of alternative catalyzer especially, dehydrogenation is effective for oxygen-free environment for it.The hydrogen that is produced by the primary alconol dehydrogenation also is useful, is used in particular for the production of fuel cell.For example W.H.Cheng is at Acc.Chem.Rev., and the 32nd rolls up, and having described primary alconol such as methanol conversion among the 685-91 (1999) is hydrogen, as various application, the particularly safety of the hydrogen fuel cell of automobile application and the source thing that can conveniently transport.

Summary of the invention

The invention provides the method for the catalyzer that can be used in various heterogeneous oxidations and the dehydrogenation reaction and these catalyzer of preparation, described reaction comprises that the catalyzed oxidation by tertiary amine prepares secondary amine and prepares carboxylic acid by the catalytic dehydrogenation of primary alconol.Described catalyzer comprises carrier, and carbon support has formed a kind of composition thereon especially, and said composition contains with nitrogen and/or carbon bonded transition metal and randomly is deposited on other metal on the modified support.Disclosed here oxide catalyst is particularly useful for forming N-((phosphonomethyl)) glycine product in the oxicracking of PMIDA reagent such as N-((phosphonomethyl)) iminodiethanoic acid.In this reaction, it is effective that catalyzer of the present invention has been proved to be in the further oxidation of catalysis formaldehyde and formic acid by product.Dehydrogenation catalyst of the present invention is particularly suitable for preparing iminodiacetic acid compounds by the catalytic dehydrogenation of diethanolamine.

Therefore, in brief, the present invention relates to comprise the catalyzer of carbon support, on carbon support, formed the transition metal composition that contains transition metal, nitrogen and carbon.In first embodiment, this catalyzer has at least about 600m ²Total Langmuir (Langmuir) surface-area of/g.In second embodiment, total Langmuir surface-area of catalyzer be carbon support before forming transition metal composition on the carbon support total Langmuir surface-area at least about 60%.In another embodiment, the micropore Langmuir surface-area of catalyzer is at least about 750m ²/ g and be carbon support before forming transition metal composition on the carbon support micropore Langmuir surface-area at least about 55%.In another embodiment, the total mesopore of catalyzer and macropore Langmuir surface-area are at least about 175m ²/ g and be the total mesopore of carbon support before forming transition metal composition on the carbon support and macropore Langmuir surface-area at least about 70%.In a further embodiment, transition metal composition is present on the carbon support with the form of discrete particle and described particulate has the granularity that is lower than about 1000nm at least about 95 weight %, by their overall dimension.

In another embodiment, this catalyzer that comprises the carbon support that has formed the transition metal composition that contains transition metal, carbon and nitrogen thereon further is included in the lip-deep carbon nanotube of carbon support.Described carbon nanotube has the diameter at least about 0.01 μ m.In another embodiment, this carbon nanotube has the diameter that is lower than about 1 μ m.

In another embodiment, this catalyst pack carbon-containing carrier has formed the transition metal composition that contains transition metal and nitrogen on this carbon support.Existing with the non-zero oxidation state of transition metal at least about 5 weight %, and this catalyzer has at least about 600m ²Total Langmuir surface-area of/g.

In another embodiment, this catalyst pack carbon-containing carrier has formed the transition metal composition that contains multiple transition metal and nitrogen on this carbon support.This catalyzer has at least about 600m ²Total Langmuir surface-area of/g.

In another embodiment, this catalyzer comprises the modification carbon support, and described modification carbon support comprises the carbon support that has formed the transition metal composition that contains transition metal, carbon and nitrogen thereon.The metal that is selected from copper, nickel, cadmium, cobalt and its mixture is deposited on the modification carbon support according to the ratio of about 2-8 weight % of this catalyzer.

In another embodiment, this catalyzer comprises the modification carbon support, and described modification carbon support comprises the carbon support that has formed the transition metal composition that contains transition metal, carbon and nitrogen thereon.Copper bearing activity is deposited on the modification carbon support mutually.

In another embodiment of the invention, this catalyst pack carbon-containing carrier has formed the transition metal composition that contains transition metal, nitrogen and carbon on this carbon support.Catalyzer is further characterized in that it is used for the validity of catalysis oxidation of formaldehyde.More particularly, when the formaldehyde that contains the 0.8 weight % that has an appointment and the representative aqueous solution with pH value of about 1.5 and oxygenant when under about 100 ℃ temperature, contacting in the presence of the described catalyzer, formaldehyde be converted to formic acid, carbonic acid gas and/or water at least about 5%.

In another embodiment, this catalyzer that comprises the carbon support that formed the transition metal composition that contains transition metal, nitrogen and carbon thereon embodies feature and is containing N-((phosphonomethyl)) iminodiethanoic acid of the formaldehyde of the 0.8 weight % that has an appointment and about 6 weight % and having the validity of catalysis oxidation of formaldehyde in the representative aqueous solution of about 1.5 pH value in it.More particularly, when the described representative aqueous solution and oxygenant when under about 100 ℃ temperature, contacting in the presence of the described catalyzer, formaldehyde be converted to formic acid, carbonic acid gas and/or water at least about 50%.

In a further embodiment, this catalyzer comprises the structure that supports that is selected from silica, aluminum oxide and the carbon support.The transition metal composition that contains transition metal, carbon and nitrogen forms on this carrier.Existing with the non-zero oxidation state of transition metal at least about 5 weight %, and this catalyzer has at least about 600m ²Total Langmuir surface-area of/g.

In another embodiment again, the catalyst pack carbon-containing carrier has formed composition on this carbon support, and said composition comprises carbon, nitrogen and is selected from element in IIA family, tellurium, selenium and its mixture.

The invention further relates to the method for the various embodiments of the aforesaid oxide catalyst of use with the organic substrates oxidation.In these class methods, organic substrates contacts in the presence of described oxide catalyst with oxygenant.

In another embodiment, the method for oxidizing organic substrates comprises allows organic substrates contact in the presence of oxide catalyst with oxygenant, this catalyst pack carbon-containing carrier and formed the transition metal composition that contains transition metal and nitrogen on this carbon support.Transition metal is selected from copper, silver, vanadium, chromium, molybdenum, tungsten, manganese, nickel, ruthenium, cerium and their mixture.

The invention further relates to the method for preparing catalyzer, this catalyst pack is contained in the transition metal composition that contains transition metal and nitrogen on the porous carbon carrier.In one embodiment, the porous carbon carrier is a particle form, and the fixed bed of granular porous carbon support or fluidized-bed contact with the vapor phase source of nitrogenous compound, wherein the precursor that has transition metal composition on described granular porous carbon support.The bed of granular porous carbon support be heated when nitrogenous compound contacts so that on carbon support, form transition metal composition.

According to another embodiment, the method for preparing catalyzer comprises allows the porous carbon carrier contact with the vapor phase source of nitrogenous compound, wherein the precursor that has transition metal composition on the carbon support of described hole.The porous carbon carrier be heated to about 600-975 ℃ temperature when nitrogenous compound contacts, thereby on carbon support, form transition metal composition.

Others of the present invention provide dehydrogenation catalyst and their method of preparation and their purposes in the reaction of catalysis primary alconol dehydrogenation production carboxylate salt.

In one embodiment, this catalyzer comprises the modification carbon support, and described modification carbon support comprises the carbon support of the composition that has formed the transition metal that contains carbon and be selected from tungsten and molybdenum thereon.The metal that is selected from IB family and the VIII family metal is deposited on the described modification carbon support.

The modification carbon catalyst support is provided in another embodiment, it comprise carbon support and on this carbon support, form contain nitrogen and be selected from the composition of the transition metal in molybdenum and the tungsten.This catalyzer can form on this modification carbon support by the metal deposition that will be selected from IB family and the VIII family metal.

The invention further relates to the method that forms catalyzer, this catalyst pack is contained in the transition metal composition on the porous carbon carrier, and this transition metal composition contains carbon and the transition metal that is selected from molybdenum and the tungsten.This method comprises allows hydrocarbon contact with the porous carbon carrier that has the transition metal composition precursor thereon, thereby produces the modification carbon support that has formed transition metal composition thereon.The metal that is selected from IB family and the VIII family metal is deposited on the described modified catalyst supports.

Another embodiment of the invention provides the method that forms catalyzer, and this catalyst pack is contained in the transition metal composition on the porous carbon carrier, and this transition metal composition contains nitrogen and the transition metal that is selected from molybdenum and the tungsten.This method comprises allows nitrogenous compound contact with the porous carbon carrier that the transition metal composition precursor is arranged thereon, thereby produces the modification carbon support that has formed transition metal composition thereon.

The invention further relates to the method for preparing carboxylate salt.This method comprises allows primary alconol contact in alkaline medium with catalyzer.This catalyst pack contains the modification carbon support that has deposited copper thereon.Described modification carbon support comprises the carbon support that has formed transition metal composition thereon.This transition metal composition contains transition metal and nitrogen or contains transition metal and carbon.

Other target of the present invention and feature are obvious with a part, and a part is pointed out below.

The accompanying drawing summary

Fig. 1 is scanning electronic microscope (SEM) image that has deposited the carbon-supported molybdenum carbide of copper thereon.

Fig. 2 is the SEM image that has deposited the carbon-supported molybdenum carbide of copper thereon.

Fig. 3 is transmission electron microscope (TEM) image that has deposited the carbon-supported molybdenum carbide of copper thereon.

Fig. 4 is the SEM image that has deposited the carbon-supported molybdenum carbide of copper thereon.

Fig. 5 is high resolution transmission electron microscope (HRTEM) image of carbon-supported molybdenum carbide.

Fig. 6 is the SEM image of carbon-supported molybdenum carbide.

Fig. 7 is the TEM image of carbon-supported molybdenum carbide.

Fig. 8 has shown the carbonic acid gas per-cent in the exhaust that is produced in N-((phosphonomethyl)) iminodiethanoic acid (PMIDA) oxidising process of using various as described in example 24 above catalyzer to carry out.

Fig. 9 has shown the carbonic acid gas distribution plan of the PMIDA oxidizing reaction that the various as described in example 25 above catalyzer of use carry out.

Figure 10 has shown the use carbonic acid gas distribution plan of a PMIDA oxidizing reaction that the kind catalyzer carries out as described in example 28 above.

Figure 11 has shown the carbonic acid gas per-cent in the exhaust that produces in PMIDA oxidising process as described in example 29 above.

Figure 12 has shown the carbonic acid gas per-cent in the exhaust that produces in PMIDA oxidising process as described in example 29 above.

Figure 13 has shown the carbonic acid gas per-cent in the exhaust that produces in PMIDA oxidising process as described in example 29 above.

Figure 14 has shown the carbonic acid gas per-cent in the exhaust that produces in PMIDA oxidising process as described in example 29 above.

Figure 15 has shown that carbonic acid gas drop point as described in example 32 above measures correlated result.

Figure 16 has shown the carbon dioxide generating amount in the PMIDA oxidising process of carrying out as described in example 34 above.

Figure 17 has shown the contrast at the pore surface area of the various catalyzer described in the embodiment 48.

Figure 18 has shown the contrast at the pore surface area of the various catalyzer described in the embodiment 48.

Figure 19-30 has shown the X-ray diffraction of the catalyst sample of methods analyst (XRD) result as described in example 50 above.

Figure 31-the 41st, the SEM image of the catalyst sample of methods analyst described in embodiment 51.

Figure 42 is the energy-dispersive X-ray analysis spectrum (EDS) of the catalyst sample of methods analyst described in embodiment 51.

Figure 43 and 44 is TEM images of the catalyst sample of methods analyst described in embodiment 51.

Figure 45 and 46 is SEM images of the catalyst sample of methods analyst described in embodiment 51.

Figure 47 and 48 is TEM images of the catalyst sample of methods analyst described in embodiment 51.

Figure 49-the 52nd, the SEM image of the catalyst sample of methods analyst described in embodiment 51.

Figure 53 and 54 is TEM images of the catalyst sample of methods analyst described in embodiment 51.

Figure 55 and 56 is x-ray photoelectron power spectrums (XPS) of the sample of methods analyst described in embodiment 52.

Detailed description of preferred embodiments

What here describe is the catalyzer that contains the transition metal composition that forms on carbon support.This catalyzer generally comprises the transition metal composition that contains transition metal and nitrogen, contains the transition metal composition of transition metal and carbon, perhaps contains the transition metal composition of transition metal, nitrogen and carbon.The transition metal composition that contains transition metal and nitrogen preferably includes transition metal nitride, and the transition metal composition that contains transition metal and carbon preferably includes transition metal carbide.The transition metal composition that contains transition metal, nitrogen and carbon can comprise transition metal nitride and transition metal carbide simultaneously, and/or transition metal carbide-nitride.

In various embodiments, described catalyzer comprises transition metal/carbon composition, and the latter comprises transition metal carbide (for example molybdenum carbide).In other embodiments, this catalyzer comprises transition metal/nitrogen composition, and the latter comprises transition metal nitride (for example molybdenum nitride).In another embodiment, this catalyzer comprises transition metal carbide (for example cobalt carbide) and transition metal nitride (for example cobalt nitride).In another embodiment again, this catalyzer comprises transition metal carbide-nitride (for example cobalt carbide-nitride).

Catalyzer of the present invention can be used for catalysis liquid phase (promptly at the aqueous solution or organic solvent) oxidizing reaction and especially the oxidation of catalytic tertiary amine (for example N-((phosphonomethyl)) iminodiethanoic acid) to produce secondary amine (for example N-((phosphonomethyl)) glycine).Advantageously; the catalyzer that is included in the transition metal composition that forms on the carbon support of the present invention is the oxidizing reaction of catalysis formaldehyde by product also, and this by product is to form in N-((phosphonomethyl)) iminodiethanoic acid is oxidized to the reaction of N-((phosphonomethyl)) glycine.

In certain embodiments, catalyzer of the present invention comprises the precious metal that is deposited on the modification carbon support, and this modification carbon support is included in the transition metal composition that forms on the carbon support.The existence of precious metal generally can strengthen this catalyzer and be oxidized to efficient in the oxidation of the formaldehyde by product in N-((phosphonomethyl)) the glycine process at N-((phosphonomethyl)) iminodiethanoic acid.Though be favourable in the oxidizing reaction of catalyzer of the present invention catalytic tertiary amine such as N-((phosphonomethyl)) iminodiethanoic acid under the situation that does not have precious metal to exist and also be that effectively existing in of noble metal active phase is preferred in some cases for the oxidation of by product such as formaldehyde.By estimating the experimental data of concrete substrate and method, employing standard economic principle, the catalyzer that those skilled in the art can weigh non precious metal are compared the advantage in productive rate, throughput, fund, depreciation, work and material cost with noble metal catalyst.

Here also described and can be used for primary alconol being changed into some catalyzer in the reaction of carboxylate salt with catalyzer, this catalyzer comprises the active phase of the containing metal (for example cupric) that is deposited on the modification carbon support, and this modification carbon support is included in the transition metal composition that forms on the carbon support.This type of catalyzer is suitable for various primary alconols are changed into carboxylate salt.Term " primary alconol " refers to comprise any alcohol of being connected to the hydroxyl on the carbon (it is bonded on two hydrogen atoms) (R-CH for example ₂OH).The dehydrogenation of primary alconol obtains carboxylate salt and hydrogen, generally carries out in containing the reacting by heating district of primary alconol, alkali and catalyzer.In various embodiments, catalyzer of the present invention is used for the diethanolamine dehydrogenation is formed Iminodiacetic acid sodium salt.

What here further describe is the method for the transition metal composition of preparation on carbon support, and said composition contains transition metal and nitrogen, transition metal and carbon, or transition metal, nitrogen and carbon.Also described in detail here is that metallic activity is deposited on method on the modification carbon support mutually, and described modification carbon support is included in the transition metal composition that forms on the carbon support.Deposit to the narration on the catalyzer that is included in the transition metal composition that carbon support (for example modification carbon support) go up to form for metallic " activity " mutually, should not be considered to get rid of the transition metal composition that on carbon support, forms or any catalytic activity of this carbon support itself.But for example known carbon support oxidation formation secondary amine and the transition metal composition of catalytic tertiary amine separately also has catalytic performance.

Generally, this supports structure and can comprise and be suitable for forming any material of transition metal composition thereon and/or be suitable for metallic activity is deposited to any material on the modified support that is included in the transition metal composition that forms on the carbon support mutually.Preferably, this supports the form that structure is a carbon support.Especially, carbon support is preferred for primary alconol being changed into carboxylate salt, and this is owing to the tolerance of carbon support to the alkaline environment of reaction.

Usually, the carbon support that is used for the present invention is to be well known in the prior art.Activation, non-graphitized carbon support are preferred.These carriers are characterised in that for the high-adsorption-capacity of gas, steam and colloidal solids and higher specific surface area.Carrier can be carbon, coke or the gac of being produced by method well known in the prior art aptly, for example by timber, peat, brown coal, coal, hard shell, bone, vegetables or other method for destructive distillation natural or synthetic carbonaceous material, but preferably in addition " activation " with the generation adsorptive power.Activation causes porous particle structure and increasing specific surface area usually with steam or be heated to high temperature (800-900 ℃) with carbonic acid gas and realize.Sometimes, hygroscopic matter, for example zinc chloride and/or phosphoric acid or sodium sulfate are added to improve loading capacity after destructive distillation or activation.Preferably, the carbon content of carbon support be from for bone black about 10% to for some charcoals about 98% and for almost being 100% from organic polymer deutero-gac.Non-carbonaceous material in being purchased absorbent charcoal material usually will be according to changing such as factors such as precursor source, processing and activation methods.Many carbon supports that are purchased contain a spot of metal.In certain embodiments, the carbon support that has minimum oxygen-containing functional group from the teeth outwards is most preferred.

The form of carbon support is not crucial.In certain embodiments, this carrier is the integrated monolithic carrier.Suitable integrated monolithic carrier can have different shape.Examples of such carriers can be for example to sieve or the form of honeycomb.Examples of such carriers also can be the form of reactor impeller for example.

In particularly preferred embodiments, this carrier is the particulate form.Because granular carrier is especially preferred, so most following discussion concentrates on the embodiment of using granular carrier.Yet should be realized that the present invention is not limited to the use of granular carrier.

Suitable granular carrier can have different shape.For example examples of such carriers can be the form of pellet.More preferably, this carrier is a form of powder.These granular carriers can be used as free particle and are used for reactor assembly, or be incorporated in addition in reactor assembly structure as the sieve or impeller on.

Typically, the carrier of particle form comprises the particle of wide size-grade distribution.For powder, preferred this particulate is about 2-300 μ m at least about 95%, by their overall dimension, more preferably this particulate is about 2-200 μ m at least about 98%, by their overall dimension and most preferably this particulate about 99% be about 2-150 μ m, by their overall dimension, wherein this particulate about 95% is about 3-100 μ m, by their overall dimension.The particle greater than about 200 μ m by its overall dimension tends to be broken into ultra-fine grain (that is, overall dimension is lower than 2 μ m), and they are difficult to reclaim.

In the following discussion, the oxidation of the specific surface area of carbon support of the present invention and dehydrogenation catalyst is according to using N ₂Well-known Langmuir method provide.Yet these values are generally corresponding to passing through to use N ₂Those values of measuring of also well-known Brunauer-Emmett-Teller (B.E.T) method.

The specific surface area of carrier is typically by using N ₂The Langmuir method measure preferably about 10-3,000m ²/ g (carbon support of the surface-area of carbon support/every gram) is more preferably about 500-2,100m ²/ g is more preferably about 750-2,100m again ²/ g.In some embodiments, most preferred specific surface area is about 750-1,750m ²/ g.In other embodiments, before forming transition metal composition on the carbon support, this particulate state carbon support typically has at least about 1000m ²/ g, more typically at least about 1200m ²/ g and more typically at least about 1400m ²The Langmuir surface-area of/g.Preferably, the Langmuir surface-area of carbon support is about 1000-1600m before forming transition metal composition on the carbon support ²/ g was about 1000-1500m before forming transition metal composition on the carbon support more preferably ²/ g.

The Langmuir micropore surface of carrier long-pending (that is, belonging to the carrier surface area that diameter is lower than the hole of 20 dusts) is typically at least about 300m ²/ g is more typically at least about 600m ²/ g.The Langmuir micropore surface amasss preferably about 300-1500m ²/ g, more preferably from about 600-1400m ²/ g.The Langmuir mesopore of the total of carrier and big aperture surface area (that is, belonging to the carrier surface area of diameter greater than the hole of 20 dusts) are typically at least about 100m ²/ g is more typically at least about 150m ²/ g.Preferably, the Langmuir mesopore of total and big aperture surface area are about 100-400m ²/ g, more preferably from about 100-300m ²/ g, 150-250m more preferably from about again ²/ g.

For some application (for example hydrogenation, oil hydrotreatment and isomerization), non-carbon support can be used with the described catalyzer that contains the transition metal composition that forms on carrier here.For example silica and alumina supporter have at least about 50m ²The Langmuir surface-area of/g.Typically, these carriers will have about 50-300m ²The Langmuir surface-area of/g.

Generally, the carrier with high surface area is preferred, because they tend to produce the finished catalyst with high surface area.

The finished catalyst that possesses enough void contents is needed, makes reactant can penetrate the hole of finished catalyst.The void content of carrier can change to a great extent.Generally, the void content of carrier is at least about 0.1cm ³/ g (carrier of void content/every gram) is typically at least about 0.5cm ³/ g.Typically, volume of voids is about 0.1-2.5cm ³/ g more typically is about 1.0-2.0cm ³/ g.Preferably, the void content of carrier is about 0.2-2.0cm ³/ g, more preferably from about 0.4-1.7cm ³/ g, 0.5-1.7cm more preferably from about again ³/ g.Comprise void content greater than about 2.5cm ³The catalyzer of the carrier of/g tends to break easily.On the other hand, comprise void content and be lower than 0.1cm ³The catalyzer of the carrier of/g tends to have little surface-area, is SA therefore.

Reactant penetrates in the hole of finished catalyst also can be influenced by the pore size distribution of carrier.Typically, carrier hole volumetrical is made up of the hole that has at least about the diameter of 20 dusts at least about 60%.Preferably, the about 60-75% of carrier hole volumetrical is made of the hole of diameter at least about 20 dusts.

Typically, carrier hole volumetrical is to be made of the hole of diameter between about 20-40 dust at least about 20%.Preferably, the about 20-35% of carrier hole volumetrical is made of the hole of diameter between about 20-40 dust.

Typically, carrier hole volumetrical is to be made of the hole of diameter at least about 40 dusts at least about 25%.Preferably, the about 25-60% of carrier hole volumetrical is made of the hole of diameter at least about 40 dusts.

Typically, carrier hole volumetrical is to be that the hole of about 40-60 dust constitutes by diameter at least about 5%.Preferably, the about 5-20% of carrier hole volumetrical is to be that the hole of about 40-60 dust constitutes by diameter.

Being used for carbon support of the present invention can be purchased from many sources.Be the tabulation of the more operable gacs of the present invention below: Darco G-60Spec and Darco X (ICI-America, Wilmington, Del.); Norit SG Extra, Norit EN4, Norit EXW, Norit A, Norit Ultra-C, Norit ACX and Norit 4x14mesh (Amer.Norit Co., Inc., Jacksonville, Fla.); G1-9615, VG-8408, VG-8590, NB-9377, XZ, NW, and JV (Barnebey-Cheney, Columbus, Ohio); BL Pulv., PWA Pulv., Calgon C 450 and PCB Fines (Pittsburgh Activated Carbon, Div.of Calgon Corporation, Pittsburgh, Pa.); P-100 (No.Amer.Carbon, Inc., Columbus, Ohio); Nuchar CN, Nuchar C-1000N, Nuchar C-190A, Nuchar C-115A and Nuchar SA-30 (Westvaco Corp., Carbon Department, Covington, Va.); Code 1551 (Baker and Adamson, Division of Allied Amer.Norit Co., Inc., Jacksonville, Fla.); Grade 235, and Grade 337, and Grade 517 and Grade 256 (Witco Chemical Corp., Activated Carbon Div., New York, N.Y.); And ColumbiaSXAC (Union Carbide New York, N.Y.).

The transition metal composition that forms on carbon support generally contains transition metal and nitrogen, contains transition metal and carbon, or contains transition metal, nitrogen and carbon.Transition metal is selected from IB family, VB family, group vib, VIIB family, VIII family, lanthanide metals and their mixture.Here the family of the element of being quoted is Chemical Abstracts Registry (CAS) system (for example VIII family comprises iron, cobalt and nickel) that is referenced as periodictable element numbering.Especially, the described metal that crosses is selected from copper, silver, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium, cerium and their mixture.In certain embodiments, this transition metal composition comprises multiple transition metal (for example cobalt and cerium).

In some other embodiment, catalyzer of the present invention comprises element that containing of forming be selected from IIA family (for example magnesium) and the VIA family (for example tellurium, the selenium) composition with nitrogen, carbon and/or nitrogen and carbon on carbon support.Catalyzer for example of the present invention can comprise the composition that contains magnesium, nitrogen and/or carbon, especially contains the composition of magnesium nitride or magnesium carbide-nitride.It should be understood that the discussion of relevant transition metal composition is equally applicable to these compositions here.

Generally, transition metal composition of the present invention comprises respectively the transition metal with form and nitrogen, carbon or carbon and the nonmetal form of nitrogen bonded (being the non-zero oxidation state) of transition metal nitride, carbide or carbide-nitride.Transition metal composition can further comprise the free transition metal that is in its metallic forms (that is zero oxidation state).This transition metal composition also can comprise the formula CN that sees service _xCarbide-combinations of nitrides thing, wherein x is about 0.01-0.7.

Typically, transition metal be to exist at least about 5 weight % with the non-zero oxidation state part of transition metal nitride, transition metal carbide or transition metal carbide-nitride (for example as), more typically at least about 20%, again more typically at least about 30%, even more typically at least about 40%.Preferably, about 5-50 weight % of transition metal is the non-zero oxidation state, more preferably from about 20-40 weight %, more preferably from about this transition metal of 30-40 weight % is the non-zero oxidation state again.

For the catalyzer that is included in the transition metal composition (for example transition metal nitride) that forms on the carbon support, transition metal composition generally account for catalyzer at least about 0.1 weight %, typically account for catalyzer at least about 0.5 weight %.Typically, this transition metal composition accounts for about 0.1-20 weight % of catalyzer, more typically accounts for about 0.5-15 weight % of catalyzer, more typically accounts for about 0.5-10 weight % of catalyzer, more typically accounts for about 1-12 weight % of catalyzer again.In certain embodiments, this transition metal composition accounts for about 1-2 weight % of catalyzer and accounts for about 1-1.5 weight % of catalyzer in other cases.

Typically, the transition metal component in the transition metal composition is to exist with the ratio at least about 0.1 weight % that is equivalent to catalyzer, more typically be equivalent to catalyzer at least about 0.5 weight %, more typically be equivalent to again catalyzer at least about 1 weight %.Preferably, this transition metal component be with about 0.1-20 weight % of being equivalent to catalyzer, more preferably be equivalent to about 0.5-10 weight % of catalyzer, the ratio that more preferably is equivalent to about 1-2 weight % of catalyzer even more preferably is equivalent to about 1-1.5 weight % of catalyzer again exists.

Contain nitrogen component in the transition metal composition of transition metal and nitrogen typically to be equivalent to the ratio at least about 0.01 weight % of catalyzer, the ratio that more typically is equivalent to catalyzer at least about 0.1 weight %, more typically be equivalent to again catalyzer at least about 0.5 weight %, even more typically be equivalent to existing of catalyzer at least about the ratio of 1 weight %.Preferably, this nitrogen component is the ratio with the about 0.1-5 weight % that is equivalent to catalyzer, the ratio that more preferably is equivalent to about 0.1-3 weight % of catalyzer more preferably is equivalent to the ratio of about 1-2 weight % of catalyzer, and the ratio that more preferably is equivalent to about 1-1.5 weight % of catalyzer again exists.

In certain embodiments, this transition metal/nitrogen composition contains cobalt and nitrogen and the cobalt nitride in various embodiments.This cobalt nitride thing typically has for example CoN _xEmpirical formula, wherein the about typically 0.25-4 of x more typically is about 0.25-2, more typically is about 0.25-1 again.Typically, has this empirical formula (Co for example ₂The overall proportion of at least a cobalt nitride N) be catalyzer at least about 0.01 weight %.Typically, the overall proportion with whole cobalt nitride of this empirical formula be catalyzer at least about 0.1 weight %.

In this type of embodiment, cobalt exists with the ratio at least about 0.1 weight % that is equivalent to catalyzer typically, more typically be equivalent to catalyzer at least about 0.5 weight %, more typically be equivalent to catalyzer at least about 1 weight %.Preferably, cobalt is the ratio with the about 0.5-10 weight % that is equivalent to catalyzer, more preferably is equivalent to the ratio of about 1-2 weight % of catalyzer, even more preferably is equivalent to the ratio existence of about 1-1.5 weight % of catalyzer.In certain embodiments, cobalt is that ratio with about 0.1-3 weight % of being equivalent to catalyzer exists.According to this type of embodiment, nitrogen is typically to be equivalent to the ratio at least about 0.01 weight % of catalyzer in addition, and the ratio that more typically is equivalent to about 0.5-2 weight % of catalyzer exists.

In certain embodiments, this transition metal/nitrogen composition contains iron and nitrogen, especially nitrided iron.This type of nitrided iron typically has for example FeN _xEmpirical formula, wherein the about typically 0.25-4 of x more typically is about 0.25-2, more typically is about 0.25-1 again.Typically, the overall proportion with at least a nitrided iron of this type of empirical formula (for example FeN) is to exist with the ratio at least about 0.01 weight % that is equivalent to catalyzer.Typically, the overall proportion with whole nitrided irons of this empirical formula be catalyzer at least about 0.1 weight %.

In this type of embodiment, iron to be equivalent to the ratio at least about 0.01 weight % of catalyzer, more typically is equivalent to the ratio at least about 0.1 weight % of catalyzer typically, and the ratio at least about 0.2 weight % that more typically is equivalent to catalyzer exists.Preferably, iron is the ratio with the about 0.1-5 weight % that is equivalent to catalyzer, the ratio that more preferably is equivalent to about 0.1-3 weight % of catalyzer more preferably is equivalent to the ratio of about 0.2-1.5 weight % of catalyzer again, even more preferably is equivalent to the ratio existence of about 0.5-1 weight % of catalyzer.In certain embodiments, iron is the ratio with the about 1-2 weight % that is equivalent to catalyzer, and the ratio that is equivalent to about 1-1.5 weight % of catalyzer in other cases exists.In addition according to this type of embodiment, nitrogen exists with the ratio that at least about 0.01 weight %, more typically is equivalent to about 0.1-2 weight % of catalyzer that is equivalent to catalyzer typically.

In certain embodiments, transition metal/carbon composition contains cobalt and carbon and contains cobalt carbide in certain embodiments.This type of cobalt carbide typically has for example CoC _xEmpirical formula, wherein the about typically 0.25-4 of x more typically is about 0.25-2, more typically is about 0.25-1 again.Typically, has this type of stoichiometry general formula (Co for example ₂The overall proportion of at least a cobalt carbide C) be catalyzer at least about 0.01 weight %.Typically, the overall proportion with whole cobalt carbides of this type of empirical formula be catalyzer at least about 0.1 weight %.

In this type of embodiment, cobalt exists with the ratio at least about 0.1 weight % that is equivalent to catalyzer typically, more typically be equivalent to catalyzer at least about 0.5 weight %, more typically be equivalent to catalyzer at least about 1 weight %.Preferably, cobalt is the ratio with the about 0.5-10 weight % that is equivalent to catalyzer, more preferably is equivalent to the ratio of about 1-2 weight % of catalyzer, even more preferably is equivalent to the ratio existence of about 1-1.5 weight % of catalyzer.In certain embodiments, cobalt is that ratio with about 0.1-3 weight % of being equivalent to catalyzer exists.

In certain embodiments, this transition metal/carbon composition contains iron and carbon, especially iron carbide.This type of iron carbide typically has for example FeC _xEmpirical formula, wherein the about typically 0.25-4 of x more typically is about 0.25-2, more typically is about 0.25-1 again.Typically, has this stoichiometry general formula (Fe for example ₃The overall proportion of at least a iron carbide C) be catalyzer at least about 0.01 weight %.Typically, the overall proportion with whole iron carbide of this empirical formula be catalyzer at least about 0.1 weight %.

In this type of embodiment, iron more typically is that the ratio at least about 0.1 weight % that is equivalent to catalyzer exists typically to be equivalent to the ratio at least about 0.01 weight % of catalyzer.Preferably, iron be with about 0.1-5 weight % of being equivalent to catalyzer, more preferably be equivalent to about 0.2-1.5 weight % of catalyzer, the ratio that more preferably is equivalent to about 0.5-1 weight % of catalyzer again exists.

It should be understood that the narration for the transition metal composition that contains iron and cobalt generally is applicable to the transition metal composition that contains above listed other transition metal (for example cerium).

In various embodiments, this transition metal composition comprises transition metal, nitrogen and carbon.In certain embodiments, this transition metal composition comprises cobalt, carbon and nitrogen, has CoC especially respectively _xOr CoN _xThe cobalt carbide of empirical formula and cobalt nitride, wherein the about typically 0.25-4 of x more typically is about 0.25-2, more typically is about 0.25-1 again.

Typically, have the cobalt carbide of this type of empirical formula and nitride and be separately to be equivalent to the ratio at least about 0.01 weight % of catalyzer, the ratio that more typically is equivalent to about 0.1-0.5 weight % of catalyzer exists.Typically, the overall proportion with whole cobalt carbides of this type of empirical formula be catalyzer at least about 0.1 weight %, and the overall proportion with whole cobalt nitride of this type of empirical formula exists with the ratio at least about 0.1 weight % of catalyzer typically.

In this type of embodiment, cobalt exists with the ratio at least about 0.1 weight % that is equivalent to catalyzer typically, more typically be equivalent to catalyzer at least about 0.5 weight %, more typically be equivalent to catalyzer at least about 1 weight %.Preferably, cobalt is the ratio with the about 0.5-10 weight % that is equivalent to catalyzer, more preferably is equivalent to the ratio of about 1-2 weight % of catalyzer, even more preferably is equivalent to the ratio existence of about 1-1.5 weight % of catalyzer.In certain embodiments, cobalt is that ratio with about 0.1-3 weight % of being equivalent to catalyzer exists.According to this type of embodiment, nitrogen is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer in addition, and the ratio that more typically is equivalent to about 0.5-2 weight % of catalyzer exists.

In certain embodiments, this transition metal composition contains iron, carbon and nitrogen, has FeC especially respectively _xOr FeN _xThe iron carbide and the nitrided iron of empirical formula, wherein the about typically 0.25-4 of x more typically is about 0.25-2, about typically again 0.25-1.For example: can have Fe ₃In addition or as an alternative, also can there be FeN in C.

Typically, have the ferrous-carbide of this type of empirical formula and nitride and be separately to be equivalent to the ratio at least about 0.01 weight % of catalyzer, the ratio that more typically is equivalent to about 0.1-0.5 weight % of catalyzer exists.Typically, the overall proportion with whole iron carbide of this type of empirical formula be catalyzer at least about 0.1 weight %, and have this type of empirical formula whole nitrided irons overall proportion typically catalyzer at least about 0.1 weight %.

In this type of embodiment, iron to be equivalent to the ratio at least about 0.1 weight % of catalyzer, more typically is equivalent to the ratio at least about 0.5 weight % of catalyzer typically, and the ratio at least about 1 weight % that more typically is equivalent to catalyzer exists.Preferably, iron is the ratio with the about 0.5-10 weight % that is equivalent to catalyzer, more preferably be equivalent to catalyzer about 1-2 weight % ratio and even the ratio that more preferably is equivalent to about 1-1.5 weight % of catalyzer exist.In certain embodiments, iron is that ratio with about 0.1-3 weight % of being equivalent to catalyzer exists.According to this type of embodiment, nitrogen is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer in addition, and the ratio that more typically is equivalent to about 0.5-2 weight % of catalyzer exists.

In various other embodiments, the transition metal composition that contains transition metal, carbon and nitrogen can comprise transition metal carbide-combinations of nitrides thing (for example cobalt carbide-nitride).For example transition metal composition can comprise cobalt carbide-nitride.In this type of embodiment, cobalt is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer, more typically be equivalent to catalyzer at least about 0.5 weight %, the ratio at least about 1 weight % that more typically is equivalent to catalyzer again exists.Preferably, cobalt is the ratio with the about 0.5-10 weight % that is equivalent to catalyzer, more preferably is equivalent to the ratio of about 1-2 weight % of catalyzer, and the ratio that more preferably is equivalent to about 1-1.5 weight % of catalyzer again exists.In certain embodiments, this cobalt carbide-nitride is that ratio with about 0.1-3 weight % of catalyzer exists.According to this type of embodiment, nitrogen is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer in addition, and the ratio that more typically is equivalent to about 0.5-2 weight % of catalyzer exists.

In various embodiments, this catalyzer can comprise cobalt carbide, cobalt nitride and cobalt carbide-nitride.In this type of embodiment, the overall proportion of this carbide, nitride and carbide-nitride typically catalyzer at least about 0.1 weight %, about 0.1-20 weight % of catalyzer typically again.

In various other embodiments, this transition metal composition can comprise ferrous-carbide-nitride.In this type of embodiment, iron is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer, the ratio that more typically is equivalent to catalyzer at least about 0.2 weight %, more typically be equivalent to the ratio at least about 0.5 weight % of catalyzer again, even more typically be equivalent to the ratio existence at least about 1 weight % of catalyzer.Preferably, iron is the ratio with the about 0.1-5 weight % that is equivalent to catalyzer, the ratio that more preferably is equivalent to about 0.1-3 weight % of catalyzer more preferably is equivalent to the ratio of about 0.2-2 weight % of catalyzer again, even more preferably is equivalent to the ratio existence of about 0.5-1.5 weight % of catalyzer.According to this type of embodiment, nitrogen is typically to be equivalent to the ratio at least about 0.1 weight % of catalyzer in addition, and the ratio that more typically is equivalent to about 0.5-2 weight % of catalyzer exists.

In various embodiments, this catalyzer can comprise iron carbide, nitrided iron and ferrous-carbide-nitride.In this type of embodiment, the overall proportion of this carbide, nitride and carbide-nitride typically catalyzer at least about 0.1 weight %, about 0.1-20 weight % of catalyzer typically again.

In various other embodiments, transition metal composition can be wrapped nickel and cobalt containing-nitride, vanadium cobalt-nitride, chromium cobalt-nitride, manganese cobalt-nitride, copper cobalt-nitride, molybdenum carbide-nitride and tungsten carbide-nitride.

According to the present invention, this transition metal composition can comprise the multiple transition metal that is selected from IB family, VB family, group vib, VIIB family, VIII family, lanthanide metals and their mixture in addition.Especially, this transition metal composition can comprise the multiple transition metal that is selected from copper, silver, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium and the cerium.For example this transition metal composition can comprise cobalt-cerium nitride, cobalt-cerium carbide and/or cobalt-cerium carbide-nitride.Other bimetal carbide-nitride that exists in transition metal composition according to the present invention can be the form of cobalt-ferrous-carbide-nitride or cobalt-copper carbide-nitride.A kind of (for example two transition metal nitride) in this type of pair transition metal composition can be to be equivalent to the ratio at least about 0.1 weight % of catalyzer, more typically, exists with the ratio of about 0.1-20 weight % of being equivalent to catalyzer.In this type of pair transition metal composition one or more (for example nitride, carbide and carbide-nitride) can be being equivalent to the ratio at least about 0.1 weight % of catalyzer, and more typical ratio with about 0.1-20 weight % of being equivalent to catalyzer exists.

In certain embodiments, the transition metal composition that on carbon support, forms generally comprise contain transition metal and carbon composition (promptly, transition metal/carbon composition) or the composition that contains transition metal and nitrogen (promptly, transition metal/nitrogen composition) any in or both, wherein this transition metal is selected from molybdenum and tungsten.The transition metal composition that contains molybdenum or tungsten that forms on carbon support can be used as oxide catalyst; Yet they can be used as the modification carbon support that is used for dehydrogenation catalyst especially.

Therefore, in some among these embodiments, transition metal/carbon composition contains molybdenum and carbon and contains molybdenum carbide in preferred embodiments.Typically, comprise as the molybdenum carbide on carbon support of a transition metal composition part and have stoichiometry formula M o ₂The compound of C.In other embodiments, transition metal/carbon composition comprises tungsten and carbon and comprises wolfram varbide in preferred embodiments.Typically, comprise as the wolfram varbide that on carbon support, forms of a transition metal composition part and have stoichiometry general formula WC or W ₂The compound of C.

Similarly, transition metal/nitrogen composition can comprise molybdenum and nitrogen and comprise molybdenum nitride in preferred embodiments.Typically, any molybdenum nitride that forms on carbon support as a transition metal composition part comprises having stoichiometry formula M o ₂The compound of N.The transition metal that forms on carbon support/nitrogen composition can comprise tungsten and nitrogen and comprise tungsten nitride in preferred embodiments.Typically, comprise as any tungsten nitride that on carbon support, forms of a transition metal composition part and have stoichiometry general formula W ₂The compound of N.

In relating to the various embodiments that comprise any in transition metal/carbon composition or the transition metal/nitrogen composition or both transition metal composition (wherein transition metal is selected from molybdenum and tungsten), this transition metal composition generally account for catalyzer at least about 5 weight %, wherein said catalyzer comprises the transition metal composition (that is modification carbon support) that forms on carbon support.This type of modification carbon support can be used as especially by metallic activity being deposited on mutually the modification carbon support in the dehydrogenation catalyst that forms on the modification carbon support.Typically, this transition metal composition accounts for about 5-20 weight % of catalyzer, more typically accounts for about 10-15 weight % of catalyzer, more typically accounts for about 10-12 weight % of catalyzer again.Generally, the transition metal component in the transition metal composition (that is, molybdenum or tungsten and nitrogen and/or carbon) account for catalyzer at least about 5 weight %.Preferably, the transition metal component in the transition metal composition accounts for about 8-15 weight % of catalyzer.

The transition metal composition that is deposited on the carbon support based on the above discussion be directed in the catalyzer that also contains the active phase of containing metal that is deposited on the modification carbon support, and wherein the modification carbon support is included in this type of transition metal composition that forms on the carbon support.

In the method that is used on carbon support forming transition metal composition, by make carbon support with containing that the source compound of wanting sedimentary transition metal to some extent contacts the precursor of formation transition metal composition on carbon support at first.

Generally, source compound is the form of water-soluble transition metal salt, is selected from halogenide, vitriol, acetate, nitrate, ammonium salt and their mixture.Typically, source compound is the form of transition metal salt, for example transition metal halide.Yet, be not crucial to the selection of transition metal salt.For example in order to produce the ferruginous transition metal composition of bag, source compound can comprise iron halide (FeCl for example ₃), ferric sulfate (FeSO for example ₄), the ammonium salt of ironic acetate, iron ((NH for example ₄) ₄Fe (CN) ₆) or their mixture.Similarly, in order to produce the transition metal composition that comprises cobalt, source compound can comprise halogenation cobalt (CoCl for example ₂), rose vitriol (CoSO for example ₄), cobaltous acetate or their mixture.Similarly, in order to produce the transition metal composition that comprises molybdenum or tungsten, the salt that contains molybdenum or tungsten is preferably water miscible, generally is selected from sodium salt, sylvite and ammonium salt.Described salt can contain the molybdenum of anionic form, for example with ammonium molybdate ((NH ₄) ₂MoO ₄ ^-2) or Sodium orthomolybdate (Na ₂MoO ₄) form.For the transition metal composition that comprises tungsten, this transition metal salt can be selected from tungsten salt, comprises for example sodium wolframate and tungstophosphoric acid.

In order to form described precursor, source compound is contacted with carbon support, perhaps preparation comprises the mixture of source compound, for example comprises the aqueous solution of the salt of transition metal, and carbon support is contacted with this type of mixture.Advantageously, this can be by the aqueous slurries of preparation particulate state carbon support in liquid medium (for example water), in slurry, add the aqueous solution that contains the salt that comprises transition metal then and finish.Perhaps, the aqueous slurries that contains the particulate state carbon support can be added in the aqueous solution that contains the salt that comprises transition metal.

The amount of the source compound that contacts with carbon support or with slurry that carbon support contacts in the amount of the source compound that exists be not very crucial.Generally, the source compound of appropriate amount should be added in any slurry that contains carbon support so that enough transition metal depositions to be provided.Typically, source compound is with at least about the speed of 0.00005 moles/min, more typically the speed with about 0.00005-0.0005 moles/min is added in the carbon support slurry.Typically, source compound is with at least about the 0.01g/ liter, more typically the ratio that rises of about 0.1-10g/ is present in the suspension or slurry that contains source compound and liquid medium.Carbon support is typically to be present in suspension or the slurry at least about 1g/ liter, the ratio that more typically rises with about 1-50g/.Preferably, source compound and carbon support are that weight ratio with the transition metal/carbon in about 0.1-20 scope is present in suspension or the slurry.More preferably, source compound and carbon support are that weight ratio with the transition metal/carbon in about 0.5-10 scope is present in suspension or the slurry.

The speed that the salt that contains transition metal is added in the slurry that contains carbon support is not very crucial, but generally is according to adding salt in the slurry (slurry of 0.01 gallons per hour/per gallon) at least about 0.05L/ hour/every L slurry.Preferably, salt from about 0.05L/ hour/every L slurry (slurry of 0.01 gallons per hour/per gallon) to about 0.4L/ hour/every L slurry (slurry of 0.1 gallons per hour/per gallon), more preferably the salt from about 0.1L/ hour/every L slurry (slurry of 0.026 gallons per hour/per gallon) to about 0.2L/ hour/every L slurry (slurry of 0.052 gallons per hour/per gallon) is added to the slurry that contains carbon support.

The transition metal composition that on carbon support, forms therein comprise the composition that contains molybdenum or tungsten and carbon contain molybdenum or the composition of tungsten and nitrogen in any or both some embodiment in, the method for precursor deposition is generally carried out based on the above discussion.Typically, the aqueous solution that contains the salt of molybdenum or tungsten is added in the aqueous slurry of particulate state carbon support.Typically, salt is with at least about the speed of 0.00005 moles/min, more typically the speed with about 0.00005-0.0005 moles/min is added in the carbon support slurry.Typically, this salt is present in suspension or the slurry, and they contain at least about 0.1g/ liter, the more typically salt and the liquid medium of the ratio that rises of about 0.1-5g/.Carbon support is typically to be present in suspension or the slurry at least about 1g/ liter, the ratio that more typically rises with about 5-20g/.Preferably, containing the salt of molybdenum or tungsten and carbon support is present in suspension or the slurry according to the molybdenum/carbon between from about 0.1 to about 20 or the weight ratio of tungsten/carbon.More preferably, containing the salt of molybdenum or tungsten and carbon support is present in suspension or the slurry according to the weight ratio of the molybdenum/carbon between from about 1 to about 10 or tungsten/carbon.Generally, the solution that contains molybdenum or the tungsten salt/every gram carbon support at least about 0.001L is added in the slurry.Preferably, about 0.001-0.05L transition metal salt/every gram carbon support is added in this slurry.This salt is present in the water-bearing media with the concentration when precursor deposition (wherein the carbon support slurry is added in the solution or suspension that contains source compound) begins typically.Perhaps, these concentration general proxies of source compound the solution of source compound or suspension are added to the cumulative total that is added to the source compound in the carbon support slurry in those embodiments in the carbon support slurry therein.

The speed of the salt that contains molybdenum or tungsten being added in the slurry is not very crucial in these embodiments, but generally at least about 0.05L/ hour every L slurry (0.01 gallons per hour/per gallon slurry) salt be added in the slurry.Preferably, salt from about 0.05L/ hour/every L slurry (0.01 gallons per hour/per gallon slurry) to about 0.4L/ hour/every L slurry (0.1 gallons per hour/per gallon slurry), more preferably the salt from about 0.1L/ hour/every L slurry (0.026 gallons per hour/per gallon slurry) to about 0.2L/ hour/every L slurry (0.052 gallons per hour/per gallon slurry) is added to the slurry.

Can believe, the pH of transition metal salt and carbon support mixture with respect to the point of zero electric charge of carbon (promptly, pH be in 3 the mixture for example carbon demonstrate zero charge, and pH greater than 3 or be lower than that carbon demonstrates negative charge and positive charge respectively in 3 the mixture) can influence contain the formation of the precursor of transition metal.The transition metal salt with metal component (for example molybdenum) that demonstrates the plus or minus electric charge can be selected, to be provided at the keyed jointing between carbon and the metal, based on the pH of carrier slurry.For example for ammonium molybdate, most molybdenum will be as MoO ₄ ^2-Exist, irrelevant with pH.Yet the pH of slurry can influence MoO ₄ ^2-Absorption on carbon surface.For example when the carbon in slurry has point of zero electric charge when pH is 3, and be that absorption situation in 5 the slurry is compared the MoO of more ratios at pH ₄ ^2-With being adsorbed on pH is on the carbon in 2 the slurry.For being ammonium tungstate or ammonium molybdate in the slurry of about 2-3 at pH, whole basically transition metal is attracted on the carbon support (that is, be lower than about 0.001% transition metal be retained in the salts solution).The pH of slurry can by with transition metal salt side by side or after transition metal salt adds end of processing in the slurry to, add acid or alkali is controlled.

Perhaps, the pH of the slurry of source compound and carbon support and and then the electric charge of carbon support can be to exist as the positively charged ion of source compound or negatively charged ion to control according to transition metal component.Therefore, when the transition metal is a positively charged ion as source compound when existing, the pH of slurry preferably remains on and is higher than 3 to promote that transition metal is adsorbed on the carbon support surface.In certain embodiments, the pH of liquid medium maintains more than 7.5 or 7.5.

In various embodiments, transition metal is as positively charged ion (FeCl for example ₃Or CoCl ₂) be present in the source compound.Along with the pH raising of liquid medium, partly hydrolysis of the transition-metal cation in the source compound.For example for FeCl ₃, can form ironic hydroxide ion such as Fe (OH) ₂ ^{+ 1}Or Fe (OH) ^{+ 2}, this type of ion is adsorbed on the electronegative carbon support surface.Preferably, ion diffusion is in hole and be adsorbed and be dispersed on the whole surface of carbon support, is included in the surface of hole.Yet, if the pH of liquid medium improves too soon, ironic hydroxide (Fe (OH) ₃) will be deposited in the liquid medium, and iron ion changes into the neutral hydrogen ferric oxide and will eliminate the electrostatic attraction between iron and carbon support surface and reduce the deposition of iron on carrier surface.Ferric hydroxide precipitate also can hinder iron ion to be dispersed in the hole on carbon support surface in liquid medium.Therefore, the pH of preferred controlled liq medium is so that utilizing electrostatic attraction between transition metal ion and the carbon support surface to avoid the rapid precipitation of transition metal hydroxide before depositing on the carbon support surface fully by transition metal.After iron deposits on the carbon support surface fully, the pH of liquid medium will improve with bigger speed, be retained in the body liquid phase because reduce the iron of ratio.

The temperature of liquid medium also influences the sedimentation speed and the following property deposition of transition metal on carbon support of transition metal.Generally, sedimentation speed will improve along with the raising of medium temperature.Typically, in the introducing process of source compound, the temperature of liquid medium is maintained at about in the 10-30 ℃ of scope, more typically is maintained at about in the 20-25 ℃ of scope.

The further embodiment that exists as the positively charged ion of source compound according to transition metal wherein, after source compound the process in the liquid medium of adding to was finished, the pH of liquid medium and temperature can improve.In certain embodiments, the pH of liquid medium brings up at least about 8.5, brings up in other embodiments at least about 9.0, in other embodiments, brings up at least about 9.0.Generally, the temperature of liquid medium is brought up at least about 40 ℃, more generally brings up at least about 45 ℃ more general again bringing up at least about 50 ℃.Typically, temperature be with about 0.5-10 ℃/minute, more typically improve with about 1-5 ℃/minute speed.

After the temperature and/or pH raising of liquid medium, this medium typically keeps suitable for some time under these conditions, so that allow transition metal deposit to fully on the carbon support surface.Typically, liquid medium kept under this condition at least about 2 minutes, more typically at least about 5 minutes, more more typically at least about 10 minutes.

In certain embodiments, the temperature of liquid medium is about 25 ℃, and the pH of liquid medium is maintained at about 7.5-8.0 in the interpolation process of source compound.After the interpolation of source compound finished, liquid medium stirred by stir about 25-35 minute, and its pH is maintained at about 7.5-8.5 simultaneously.The temperature of liquid medium is brought up to about 40-50 ℃ temperature then with about 1-5 ℃/minute speed, the pH of liquid medium is maintained at about 7.5-8.5 simultaneously.This medium stirred by stir about 15-25 minute, and simultaneously the temperature of liquid medium is maintained at about 40-50 ℃ and pH and is maintained at about 7.5-8.0.Slurry is heated to about 50-55 ℃ temperature then and its pH regulator arrives about 8.5-9.0, and these conditions kept about 15-25 minute.At last, this slurry is heated to about 55 ℃-65 ℃ temperature and its pH regulator arrives about 9.0-9.5, and these conditions kept about 10 minutes.

Do not consider transition metal existence in source compound as negatively charged ion or positively charged ion, in order to promote contacting and promote mass transfer from liquid phase between carrier and the transition metal source compound, when adding to source compound in the slurry or after transition metal salt being added in the slurry, this slurry is stirred.This liquid medium can or be stirred before for the temperature that improves it and/or operation that pH carried out, in the process equally afterwards.Suitable stirring mode comprises for example stirring or this slurry of shake.

For the transition metal composition that contains multiple metal, according to the discussion of front, typically, the single multiple source compound of planting source compound or containing at least a described metal separately that contains whole these metals contacts with carbon support.The deposition of the precursor of component transition metal can be based on the above discussion method (promptly side by side, allow carbon support contact with multiple source compound, these source compounds contain the transition metal of using for precursor deposition separately) or sequentially (deposit a kind of precursor, deposit one or more additional precursors then) and carry out.

Transition metal salt contacted the abundant deposition that has reached the sufficient to guarantee source compound and/or forms its for some time of (they) derivative with carrier after, slurry filtered, this carrier solution washing, and dry.Typically, salt contacted with carrier at least about 0.5 hour, more typically was about 0.5-5 hour.Generally, the carrier drying of process dipping was at least about 2 hours.Preferably, the about 5-12 of carrier drying hour of the process dipping.Drying process can obtain quickening by allowing impregnated carbon support contact under general about 80-150 ℃ temperature with air.

Also can form source compound or derivative on carbon support by vapor deposition process, carbon support contacts with the mixture in the vapor phase source that comprises transition metal in these methods.In chemical vapour desposition, carbon support contacts with volatile metal compounds in generally being selected from halogenide, carboxide and organometallic compound, and these compounds can decompose and produce the transition metal that is adapted at forming on the carbon support.The example of suitable metal carbonyl comprises Mo (CO) ₆, W (CO) ₆, Fe (CO) ₅And Co (CO) ₄

Generally by allowing compound be exposed to light or heat with compound decomposition.For the decomposition of using heating, break down typical ground need be at least about 100 ℃ temperature.

Should be pointed out that precursor compound can be identical with source compound, perhaps owing in deposition process and/or in addition, making them different with nitrogenous compound, carbon compound (for example hydrocarbon) or the nitrogenous chemical transformation that contacts generation before with carbon compound.For example comprise aqueous solution when dipping of the source compound of ammonium molybdate when porous carbon supported body and function, precursor is identical with source compound usually.But when for example the halogenation molybdenum used vapor deposition techniques for source compound, the precursor of formation can be metal molybdenum or molybdenum oxide.

Do not consider on carbon support to form the method for source compound or derivatives thereof, pretreated in certain embodiments carbon support is accepted further processing (for example processing of programmable temperature) then and is comprised transition metal and nitrogen, comprises transition metal and carbon or comprise the transition metal composition of transition metal, nitrogen and carbon so that form on carbon support.Generally, pretreated carbon support and nitrogenous, carbon containing or nitrogenous and carbon compound under certain condition (for example temperature of Sheng Gaoing) contact.Generally, fixed bed or the fluidized-bed that comprises the carbon support that has deposited precursor contacts with nitrogenous and/or carbonaceous compound.Preferably, carbon support is arranged in the fixed-bed reactor, and nitrogenous, the carbon containing of vapour phase or nitrogenous and carbon compound by on the bed of carbon support through and/or the bed that passes carbon support contact with carbon support.

When needs comprise the transition metal composition of transition metal and nitrogen, typically, any contact in pretreated carbon support and the various nitrogenous compounds, these nitrogenous compounds comprise ammonia, amine, nitrile, nitrogenous heterogeneous ring compound, or their mixture.This type of nitrogenous compound typically is selected from ammonia, dimethyl amine, quadrol, Isopropylamine, butylamine, melamine, acetonitrile, propionitrile, pyridine carbonitrile (picolonitrile), pyridine, pyrroles and their mixture.

Typically, the carbon support that has deposited the transition metal composition precursor contacts with the nitriding atmosphere that comprises above-mentioned vapour phase nitrogenous compound.In preferred embodiments, nitrogenous compound comprises acetonitrile.Typically, this nitriding atmosphere comprises the nitrogenous compound at least about 5 volume %, the nitrogenous compound of more typically about 5-20 volume %.Generally, at least about the carbon of nitrogenous compound/every kg of 100 liters/per hour (at least about 3.50ft ³The carbon/per hour of carbon compound/every lb) contact with carbon support.Preferably, (the about 7.0-17.7ft of the carbon of nitrogenous compound/every kg of rising of about 200-500/per hour ³The carbon/per hour of carbon compound/every lb) contact with carbon support.

The optional annexing ingredient that is selected from hydrogen and rare gas element such as the argon gas that comprises of this nitriding atmosphere.When having hydrogen, generally with at least about 1 volume % hydrogen or more generally exist with the ratio of about 1-10 volume % hydrogen.In addition or as an alternative, this nitriding atmosphere typically comprises at least about 75 volume % argon gas, more typically about 75-95 volume % argon gas.In certain embodiments, this nitriding atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb).Preferably, this nitriding atmosphere comprises (the about 1.05-1.8ft of the carbon support of hydrogen/every kg that about 30-50 rises/per hour ³The carbon support/per hour of hydrogen/every lb).In various other embodiments, this nitriding atmosphere comprises carbon support at least about argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).Preferably, this nitriding atmosphere comprises (the about 63-160ft of the carbon support of argon gas/every kg that about 1800-4500 rises/per hour ³The carbon support/per hour of argon gas/every lb).In other embodiments, this nitriding atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb) with at least about the carbon support of argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).

The carbon support that deposits the transition metal composition precursor typically is being not more than under about 15 pounds/square inch total pressure in the nitrogenizing reaction district with nitrogenous compound and is contacting.Typically, this nitrogenizing reaction district is under the pressure of about 2-15 pound/square inch.The nitrogenous compound dividing potential drop in nitrogenizing reaction district typically is not more than about 2 pounds/square inch, more typically is about 1-2 pound/square inch.The dividing potential drop of any hydrogen that exists in the nitrogenize section typically is lower than about 1 pound/square inch, more typically is about 0.1-1 pound/square inch.

When needs comprised the transition metal composition of transition metal and carbon, typically, pretreated carbon support contacted with the carburizing atmosphere that contains carbon compound (comprising for example hydro carbons, as methane, ethane, propane, butane and pentane).

Typically, the carbon support that deposits the transition metal composition precursor contacts with the carburizing atmosphere that comprises the vapour phase carbon compound.In preferred embodiments, carbon compound comprises methane.Typically, this carburizing atmosphere comprises the carbon compound at least about 5 volume %, the carbon compound of more typically about 5-50 volume %.Generally, at least about the carbon of carbon compound/every kg of 100 liters/per hour (at least about 3.50ft ³The carbon/per hour of carbon compound/every lb) contact with carbon support.Preferably, (the about 7.0-17.7ft of the carbon of carbon compound/every kg of rising of about 200-500/per hour ³The carbon/per hour of carbon compound/every lb) contact with carbon support.

The optional annexing ingredient that is selected from hydrogen and rare gas element such as argon gas and the nitrogen that comprises of this carburizing atmosphere.When having hydrogen, generally exist with ratio at least about 1 volume % or more generally about 1-50 volume %.In certain embodiments, this carburizing atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb).Preferably, this carburizing atmosphere comprises (the about 1.05-1.8ft of the carbon support of hydrogen/every kg that about 30-50 rises/per hour ³The carbon support/per hour of hydrogen/every lb).

In various other embodiments, this carburizing atmosphere comprises carbon support at least about argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).Preferably, this carburizing atmosphere comprises (the about 63-160ft of the carbon support of argon gas/every kg that about 1800-4500 rises/per hour ³The carbon support/per hour of argon gas/every lb).

In other embodiments, this carburizing atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb) with at least about the carbon support of argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).

In various other embodiments, this carburizing atmosphere comprises carbon support at least about nitrogen/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of nitrogen/every lb).Preferably, this carburizing atmosphere comprises (the about 63-160ft of the carbon support of nitrogen/every kg that about 1800-4500 rises/per hour ³The carbon support/per hour of nitrogen/every lb).

The carbon support that deposits the precursor of transition metal composition typically is being not more than under about 15 pounds/square inch total pressure in the carburizing reagent district with carbon compound and is contacting.Typically, this carburizing reagent district is under the pressure of about 2-15 pound/square inch.The carbon compound dividing potential drop in carburizing reagent district typically is not more than about 2 pounds/square inch, more typically is about 1-2 pound/square inch.The dividing potential drop of any hydrogen that exists in the carburizing reagent district typically is lower than about 2 pounds/square inch, more typically is about 0.1-2 pound/square inch.

In certain embodiments, pretreated carbon support (having the precursor transistion metal compound thereon) can be handled so that form the transition metal composition that comprises carbon and nitrogen and transition metal simultaneously on carbon support.In this type of embodiment, the precursor compound on carrier can contact with " carbonization-nitriding atmosphere ".A kind of method comprises allows pretreated carbon support contact with nitrogen compound with carbon containing.Suitable carbon containing and nitrogen compound comprise amine, nitrile, nitrogenous heterogeneous ring compound or their mixture.This type of carbon containing and nitrogen compound generally are selected from dimethylamine, quadrol, Isopropylamine, butylamine, melamine, acetonitrile, propionitrile, pyridine carbonitrile, pyridine, pyrroles and their mixture.

Typically, the carbon support that deposits the transition metal composition precursor contacts with the carbonization-nitriding atmosphere that comprises vapour phase carbon containing and nitrogen compound.Typically, carbonization-nitriding atmosphere comprises at least about the carbon containing of 5 volume % and nitrogen compound, carbon containing and the nitrogen compound of more typically about 5-20 volume %.Generally, at least about 100 liters carbon containing and the carbon of nitrogen compound/every kg/per hour (at least about 3.50ft ³Carbon containing and the carbon of nitrogen compound/every lb/per hour) contact with carbon support.Preferably, (the about 7.0-17.7ft of the carbon of the carbon containing that rises of about 200-500 and nitrogen compound/every kg/per hour ³Carbon containing and the carbon of nitrogen compound/every lb/per hour) contact with carbon support.

The optional annexing ingredient that is selected from hydrogen and rare gas element such as the argon gas that comprises of carbonization-nitriding atmosphere.When having hydrogen, generally exist with ratio at least about 1 volume % or more generally about 1-5 volume %.In certain embodiments, this carbonization-nitriding atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb).Preferably, this carbonization-nitriding atmosphere comprises (the about 1.05-1.8ft of the carbon support of hydrogen/every kg that about 30-50 rises/per hour ³The carbon support/per hour of hydrogen/every lb).

In various other embodiments, this carbonization-nitriding atmosphere comprises carbon support at least about argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).Preferably, this carbonization-nitriding atmosphere comprises (the about 63-160ft of the carbon support of argon gas/every kg that about 1800-4500 rises/per hour ³The carbon support/per hour of argon gas/every lb).

In other embodiments, this carbonization-nitriding atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support of hydrogen/every lb) with at least about the carbon support of argon gas/every kg of 900 liters/per hour (at least about 31.5ft ³The carbon support of argon gas/every lb).

The carbon support that has the transition metal composition precursor thereon typically is being not more than under about 15 pounds/square inch total pressure in carbonization-nitrogenizing reaction district with nitrogen compound with carbon containing and is contacting.Typically, this carbonization-nitrogenizing reaction district is under the pressure of about 2-15 pound/square inch.The carbon containing in carbonization-nitrogenizing reaction district and nitrogen compound dividing potential drop typically are not more than about 2 pounds/square inch, more typically are about 1-2 pound/square inches.The dividing potential drop of any hydrogen that exists in carbonization-nitrogenizing reaction district typically is lower than about 1 pound/square inch, more typically is about 0.1-1 pound/square inch.

In addition or or as an alternative, the transition metal composition that comprises transition metal, carbon and nitrogen can form by carrier is contacted with aforesaid nitrogenous compound with precursor, wherein the carbon of transition metal composition is to be derived to support structure.

In other embodiments, the precursor of carrier and transition metal composition can contact with carbon compound (for example methane) with above-described nitrogenous compound (for example ammonia) so that form the transition metal composition that comprises transition metal, carbon and nitrogen on carbon support.

In other embodiments, carbon support with comprise transition metal, nitrogen and carbon compound and contact (promptly with the precursor that on carbon support, forms transition metal composition, source compound and carbon containing and nitrogen compound are to be provided by a kind of composition), and according to following narration heating so that on carbon support, form the transition metal composition that comprises transition metal, nitrogen and carbon.Typically, this based composition comprises co-ordination complex, and described co-ordination complex contains nitrogenous organic ligand, and this part comprises and for example comprises nitrogenous five Yuans or the nitrogenous organic ligand of six element heterocycles.Generally, this type of part is selected from porphyrin, derivatives of porphyrin, polyacrylonitrile, phthalocyanine, pyrroles, the pyrroles of replacement, polypyrrole, pyridine, the pyridine of replacement, dipyridyl, phthalocyanine, imidazoles, the imidazoles of replacement, pyrimidine, the pyrimidine of replacement, acetonitrile, O-Phenylene Diamine, two pyridines, salen part, Ursol D, cyclams and their mixture.In certain embodiments, this co-ordination complex comprises phthalocyanine (for example transition metal phthalocyanine) or phthalocyanine derivates.In these co-ordination complexs some also is described among international publication No.WO 03/068387A1 and the US application publication thing No.2004/0010160A1, and their whole disclosures are hereby incorporated by reference.

In order to deposit described transition metal composition precursor in this embodiment, typically, preparation comprises the suspension of carbon support and co-ordination complex, and its is stirred one section is enough to allow coordination compound be adsorbed on time on the carbon support.Typically, this suspension contains the coordination compound of the ratio of the carbon support of the ratio that the 5-20g/ that has an appointment rises and about 2-5g/ liter.Preferably, carbon support and coordination compound are according to about 2-5, the more preferably from about weight ratio existence of 3-4.

Transition metal composition the formation on the carbon support be by in the presence of aforesaid atmosphere (that is, in the presence of nitrogenous, carbon containing or nitrogenous and carbon compound) heat this carrier and precursor carries out.Typically, has the carbon support of precursor thereon by using any heating the in the variety of way well known in the prior art, comprising for example resistance furnace or induction furnace.

Generally, the transition metal composition precursor can contain transition metal salt, the transition metal of partial hydrolysis, and/or transition metal oxide.For example for iron, this precursor can comprise FeCl ₃, Fe (OH) ₃, Fe (OH) ₂ ^{+ 1}, Fe (OH) ^{+ 2}And/or Fe ₂O ₃Generally, by providing key to substitute the key energy needed between other component in transition metal and precursor composition in order to be used between transition metal and nitrogen, carbon or carbon and the nitrogen, heating has the carbon support of transition metal composition precursor thereon, has formed transition metal composition.In addition or as an alternative, this transition metal composition can followingly form: by transition metal oxide is reduced into transition metal, the latter combines with carbon and/or nitrogen in the composition that exists in nitrogenize, carbonization or carbonization-nitriding atmosphere, and wherein carbon support is in contact with it and forms this transition metal composition.

Typically, this carrier is heated to the temperature at least about 600 ℃, more typically is heated to the temperature at least about 700 ℃, more typically is heated to the temperature at least about 800 ℃ again, even more typically be heated to temperature at least about 850 ℃, with the production transition metal composition.

The top temperature that carrier is heated to does not have strict restriction, as long as it is enough to produce transition metal nitride, transition metal carbide or transition metal carbide-nitride.Carrier can be heated to greater than 1000 ℃, greater than 1250 ℃ or about at the most 1500 ℃ temperature.Yet observe,, the greying of carbon support takes place if carrier is heated above 900 ℃ or be higher than 1000 ℃ temperature.Greying has adverse influence for catalyst activity.Therefore, preferably this carrier is heated to and is not more than about 1000 ℃ temperature.Yet, by being heated to, carrier and precursor surpass 1000 ℃ temperature, do not consider any greying may take place, can prepare active catalyst.Preferably, this carrier is heated to about 600 ℃-1000 ℃, and more preferably from about 600-975 ℃, more preferably from about 700-975 ℃, more preferably from about 800-975 ℃, 850-975 ℃ temperature more preferably from about especially is heated to about 850 ℃-950 ℃ temperature again.

For the carburizing atmosphere that comprises hydro carbons (for example methane), observed and carbon support is heated to above 700 ℃ temperature can causes on carbon support, forming polymkeric substance carbon.Therefore, comprise in some embodiment of transition metal composition of transition metal and carbon, preferably form said composition by the temperature that carrier is heated to about 600-700 ℃ in demand.The formation that it should be understood, however, that the transition metal composition that comprises transition metal and carbon is to carry out under 700 ℃ the temperature and this method is produced suitable modification carbon support and used for the present invention being higher than, and precondition is T _MaxBe enough to make carbide to form (for example at least 500 ℃ or at least 600 ℃).

Rate of heating is not very crucial equally.Typically, the carrier that has deposited precursor thereon under at least about 2 ℃/minute speed, more typically at least about 5 ℃/minute, more more typically at least about 10 ℃/minute even more typically under at least about 12 ℃/minute speed, heat.Generally, the carrier that deposits precursor thereon is under about 2-15 ℃/minute the speed, more generally heat under about 5-15 ℃/minute speed.

The carbon support that has formed transition metal/nitrogen composition and/or transition metal/carbon composition thereon can be used as the modification carbon support of the active phase of containing metal of effective promotion dehydrogenating alcohol.In various embodiments, metallic activity comprises copper mutually.

In certain embodiments of the invention, wish to form carbon containing or nitrogen (that is, transition metal carbide or the nitride) transition metal composition that comprises molybdenum or tungsten (that is, molybdenum carbide, wolfram varbide, molybdenum nitride or tungsten nitride).The method that forms this carbide and nitride comprises the reduction of programmable temperature (TPR), and it comprises allows carrier and transition metal precursors and carbonization (that is carbon containing) or nitrogenize (that is, nitrogenous) atmosphere contact under condition as described below.It should be understood that the following discussion that contains the transition metal composition of molybdenum and tungsten about formation does not limit abovely comprises at least a given discussion of catalytic activity transition metal composition in the multiple transition metal (comprising molybdenum and tungsten) about formation.

In the embodiment that needs molybdenum carbide or wolfram varbide, typically, carburizing atmosphere comprises the hydrocarbon with 1-5 carbon atom.In preferred embodiments, carbon compound comprises methane.Typically, this carburizing atmosphere comprises the carbon compound at least about 5 volume %, the carbon compound of more typically about 5-50 volume %.Generally, at least about the carbon of carbon compound/every kg of 100 liters/per hour (at least about 3.50ft ³The carbon/per hour of carbon compound/every lb) contact with carbon support.Preferably, (the about 7.0-17.7ft of the carbon of carbon compound/every kg of rising of about 200-500/per hour ³The carbon/per hour of carbon compound/every lb) contact with carbon support.

The optional annexing ingredient that is selected from hydrogen and rare gas element such as argon gas or the nitrogen that comprises of this carburizing atmosphere.When having hydrogen, generally be with at least about 1 volume % hydrogen or usually exist with the ratio of about 1-50 volume % hydrogen.In a kind of this type of embodiment, carburizing atmosphere comprises carbon support at least about hydrogen/every kg of 10 liters/per hour (at least about 0.35ft ³The carbon support/per hour of hydrogen/every lb).Preferably, this carburizing atmosphere comprises (the about 1.05-1.8ft of the carbon support of hydrogen/every kg that about 30-50 rises/per hour ³The carbon support/per hour of hydrogen/every lb).

In needing this type of embodiment of molybdenum nitride or tungsten nitride, nitriding atmosphere generally comprises nitrogenous compound such as ammonia, also can comprise rare gas element such as argon gas and nitrogen.Typically, this nitriding atmosphere comprises the nitrogenous compound at least about 5 volume %, the nitrogenous compound of more typically about 5-20 volume %.Generally, at least about the carbon of nitrogenous compound/every kg of 100 liters/per hour (at least about 3.50ft ³The carbon of nitrogenous compound/every lb) contact with carbon support.Preferably, (the about 7.1-17.7ft of the carbon of nitrogenous compound/every kg of rising of about 200-500/per hour ³The carbon/per hour of nitrogenous compound/every lb) contact with carbon support.When having hydrogen, generally exist with ratio at least about 1 volume % hydrogen or usually about 1-5 volume % hydrogen.

Comprise in the various embodiments of transition metal composition of molybdenum or tungsten at needs, the temperature of atmosphere is through t after a while ₁Bring up to and have at least about 250 ℃, 300 ℃ the temperature T of numerical value more typically ₁Preferably, the temperature of atmosphere is at t ₁In bring up to about 250 ℃-350 ℃, more preferably bring up to about 275 ℃-325 ℃.With temperature from T ₀Bring up to T ₁Needed (t during this period of time ₁) generally be at least about 5 minutes.Typically, t ₁Being about 30 minutes of about 5-, more typically is about 10-15 minute.At t ₁The speed of middle elevated temperature is not very crucial, generally is lower than 150 ℃/minute.Typically, at t ₁In temperature increase rate be about 10-100 ℃/minute, more typically be about 20-50 ℃.

At t ₁During this time, source compound or deutero-transition metal carbide or nitride can be transformed into the intermediate oxide that forms on carrier surface.At t ₁The intermediate oxide that forms in the process formula A that generally sees service _xO _y, wherein A is molybdenum or tungsten, depends on the required composition of transition metal composition.Typically, the ratio of x and y is at least about 0.33: 1, preferably about 0.33: 1 to about 1: 1.

For example in the formation of the transition metal composition that comprises molybdenum, oxide intermediate can form according to following method:

Can typically in alkaline environment, carry out by the promoted dehydrogenation reaction of catalyzer that comprises the modification carbon support (that is, being formed with the carbon support of transition metal/nitrogen composition and/or transition metal/carbon composition thereon) that deposits the active phase of containing metal (for example cupric).Because the unstable of oxide compound, the transition metal oxide precursor that does not get transformed into carbide or nitride can react the formation transition metal salt with the basic component of this dehydrogenation systems or the basic component of metal deposition solution, thereby causes transition metal to be removed from the carbon support surface.For example do not get transformed into the MoO of molybdenum carbide ₃Can react according to following reaction mechanism and sodium hydroxide:

MoO ₃+2NaOH→Na ₂MoO ₄+H ₂O

Transition metal salt is disadvantageous from lip-deep the removing of carbon support, because the catalytic performance of this infringement transition metal composition, and/or cause metallic active deposition on transition metal composition to reduce.

Therefore, according to above consideration, a high proportion of as far as possible any transition metal oxide that hope will form in carbonization or nitrogenize operation is transformed.Typically, transition metal oxide at least about 80%, more typically about 80-95% is converted to transition metal composition.Preferably, about 5 weight % that are no more than of oxide precursor remain unconvertedly, and more preferably, the about 3 weight % of being no more than in the oxide precursor keep unconverted, and more preferably the about 1 weight % that is no more than in the oxide precursor keeps unconverted again.

Relevant initial temperature (T ₀), from T ₀Be increased to T ₁Speed (t ₁), T ₁Value and the general and relevant factor of the Consideration that forms of precursor from precursor or intermediate oxide formation carbide and nitride identical.Yet the remainder of the method for reducing of programmable temperature is different on some importance, as required carbide or nitride.

Following discussion relates to the preparation of modification carbon support, and it can be as the carrier in the active phase of the containing metal that is used for promoting the alcohol dehydrogenase catalyst for reaction.Initial period (t in the temperature rising ₁, it typically causes the formation of transition metal oxide precursor) afterwards, the temperature of carbonization (that is carburizing) atmosphere is from T ₁Be elevated to top temperature (T _Max), in during this period of time, the reduction by the transition metal oxide precursor forms the transition metal carbide that contains molybdenum or tungsten on the surface of carbon support.

Typically, T _MaxBe at least about 500 ℃, more typically at least about 600 ℃, more more typically at least about 700 ℃, even more typically at least about 800 ℃ or at least about 850 ℃.Preferably, T _MaxBe about 600 ℃-1000 ℃, more preferably from about 850 ℃-950 ℃.

For the carburizing atmosphere that comprises hydrocarbon (for example methane), observed and carbon support is heated to above 700 ℃ temperature can causes on carbon support, forming polymkeric substance carbon.Therefore, comprise in some embodiment of transition metal composition of transition metal and carbon, preferably form said composition by the temperature that carrier is heated to about 600-700 ℃ at needs.The formation that it should be understood, however, that the transition metal composition that comprises transition metal and carbon is to carry out under 700 ℃ the temperature and this method is produced suitable modification carbon support and used for the present invention being higher than, and precondition is T _MaxBe enough to make carbide to form (for example at least 500 ℃ or at least 600 ℃).

Comprise in some embodiment of methane for example at carburizing atmosphere, this precursor is heated to 650 ℃ with the speed at least about 2 ℃/minute.Although be not very crucial, this precursor typically through at least about 10 minutes, more typically about 15-150 minute, more typically be about 30-60 minute time (t again ₂) be heated to T _MaxTemperature is from T ₁Bring up to T _MaxSpeed be not very crucial, but generally be at least about 2 ℃/minute.Typically, this speed is about 2-40 ℃/minute, more typically is about 5-10 ℃/minute.

Reach T in the atmosphere that contacts with oxidiferous precursor _MaxAfterwards, the temperature of atmosphere is generally at T _MaxUnder keep for some time, the required reduction of this time sufficient to guarantee transition metal oxide is to form transition metal carbide.Typically, at T _MaxUnder this section hold-time t ₃(this section in the period temperature remain on T _Max) be at least about 1 hour, can be about 1-8 hour; Yet, preferably carefully guarantee t ₃Not to make the time span of on the carbon support polymkeric substance carbon of the amount of formation meeting disadvantageous effect catalyst activity.Preferably, t ₃Be about 1-4 hour, more preferably from about 2-3 hour.

Generally, intermediate transition metal oxide and hydrocarbon contact under the condition that forms polymkeric substance carbon on the transition metal carbide surface avoiding basically.

Transition metal oxide typically is being not more than under about 15 pounds/square inch total pressure in the carburizing reagent district with hydrocarbon and is contacting.Typically, this carburizing reagent district is under the pressure of about 2-15 pound/square inch.The hydrocarbon partial pressure in carburizing reagent district typically is not more than about 2 pounds/square inch, more typically is about 1-2 pound/square inch.

T _MaxWith at T _MaxUnder hold-time t ₃All directly influence the formation of carbide, wherein each condition is controlled to realize that enough carbide form.Yet, guarantee that two conditions all can provide even preferred condition for carbide forms within preferred range.Therefore, in particularly preferred embodiments, T _MaxBe about 625-675 ℃, and t ₃It is about 2-3 hour.

Initial period t in the temperature rising ₁(it typically causes forming transition metal oxide), the temperature of nitrogenize (that is nitriding) atmosphere was from T afterwards ₁Be elevated to top temperature (T _Max), thereby form the transition metal nitride that contains molybdenum or tungsten.Form described method for carbide and compare with above, the temperature of nitriding atmosphere is then from T ₁Be elevated to top temperature (T at least about 700 ℃ _Max) to produce nitride, because observe, be lower than under 700 ℃ the temperature, the formation of nitride is not fully completely.Yet along with the approaching about temperature more than 900 ℃ and 900 ℃ of nitriding atmosphere, metal nitride is decomposed the hydrogen reducing that is produced by nitriding gas.Therefore, T _MaxPreferably about 700-900 ℃, more preferably from about 700-850 ℃, more preferably from about 725-800 ℃ again.Although be not very crucial, typically, this oxidiferous precursor is through at least about 15 minutes, more typically about 15-250 minute, more typically about 30-60 minute for some time (t again ₂) be heated to T _MaxTemperature is from T ₁Bring up to T _MaxSpeed be not very crucial, but generally be at least about 2 ℃/minute.Typically, this speed is about 2-40 ℃/minute, more typically is about 5-10 ℃/minute.

Reach T in the atmosphere that contacts with oxidiferous precursor _MaxAfterwards, the temperature of atmosphere is generally at T _MaxUnder keep for some time, the desirable transition metal oxide of this time sufficient to guarantee is reduced into transition metal nitride.Typically, this section period t ₃(temperature remains on T in this process _Max) be at least about 1 hour.Preferably, t ₃Preferably about 1-5 hour, more preferably from about 3-4 hour.

For the formation of carbide, T _MaxWith at T _MaxUnder hold-time t ₃The both directly influences nitride and forms, and wherein each condition is controlled so that realize enough nitride and formed.Yet, guarantee that two conditions all can provide even preferred condition for nitride forms within preferred range.Therefore, in particularly preferred embodiments, T _MaxBe about 725-800 ℃, and t ₃It is about 1-5 hour.

Observed the programmable temperature reduction process that nitrogen containing atmosphere bag therein is ammoniated, be used for producing transition metal nitride, formed transition metal nitride (for example molybdenum nitride) can be reduced and form the free transition metal.

2MN+2NH ₃→2M ₂+N ₂+2H ₂O

Typically generation when nitrogenizing reaction is finished of this reaction (, whole basically oxide precursors are reduced into nitride) and at T _MaxReaching comparatively high temps (that is, being higher than 900 ℃) time takes place probably.Even these reactions can be produced required transition metal nitride by the forward reaction between free transition metal and ammonia, but preferably should avoid the condition of the direct ammonia nitriding effect of free transition metal, this is by the reverse reductive possibility of hydrogen owing to nitride.This is the T by will be in nitridation process typically _MaxKeep below and to quicken the control of getting off of that temperature that ammonia is decomposed to form hydrogen, thereby prevent owing to nitride is caused reverse formation free transition metal by hydrogen reducing.

Carbonization or nitriding atmosphere and contacting of carrier can utilize fluidized-bed reaction indoor at least about 0.01 second ^-1The vapor phase stream of space velocity carry out.Vapor phase stream at indoor carbonization of fluidized-bed reaction or nitriding atmosphere is not very crucial, can demonstrate about 0.01-0.50 second ^-1Space velocity.Though the formation of carbide and nitride can easily be carried out in wide gas phase flow rates, this flow velocity can improve so that increase the diffusion of source compound in the carrier hole at first, thereby the formation of accelerated carbonation thing or nitride and shortening remain on T with temperature _MaxGuarantee that down enough carbide or nitride form the needed time.

Except that the method for reducing of programmable temperature, also can use other method of producing transition metal (for example molybdenum or tungsten) carbide.For example can under the temperature between about 500-1400 ℃, contact with rare gas element according to the above carbon support that has formed precursor from the teeth outwards.Can believe that this precursor is reduced by carbon support under hot conditions, thereby and the reaction of precursor and carbon support on the surface of carrier, form carbide.Rare gas element can be selected from argon gas, nitrogen and helium.

Another kind method comprises allowing and contacts with the reduction volatilization metallic compound under volatile metal compounds and the temperature of carbon support in about 500-1400 ℃ scope, forms compound with the carbon support reaction then.Volatile metal compounds generally is an organometallic compound.

The carbon support that has formed precursor from the teeth outwards also can contact with hydrogen (typically about 800 ℃) under about 500-1200 ℃ temperature reducing this precursor, thereby the latter and carbon support reaction form carbide on the surface of carbon support.

The time that reaches time, the top temperature itself of top temperature or temperature is remained under the top temperature is not very crucial, can be according to any variation to a great extent in these methods.

Observe, compare with the carbide that the program control reduction method of use temperature is produced, use the productive rate of the carbide of producing for the replacement scheme of the program control reduction method of said temperature and stability (for example anti-lixiviate performance under alkaline dehydrogenation or metal deposition condition) to understand decline.Therefore, the reduction method of programmable temperature is the preferred method that carbide forms.

Forming transition metal (for example molybdenum or tungsten) carbide and nitride on the carbon support surface can generally carry out based on the above discussion.The preparation method of illustrative forms transition metal (that is, molybdenum or tungsten) carbide and nitride on the aforesaid carbon support surface that deposits the precursor that contains molybdenum or tungsten from the teeth outwards.The organic ligand that a kind of these class methods are included in carbon containing and nitrogen exists allows carbon support experience high temperature (for example about 600-1000 ℃) down, thereby forms carbide and nitride on carrier surface simultaneously.Possible part comprises for example transition metal porphyrin or nitrogenous molybdenum organometallic compound (for example molybdenum pyridine compounds).

Comprise in other replacement scheme of modification carbon support of transition metal carbide and transition metal nitride in preparation, contain the transition metal nitride of (for example containing molybdenum or tungsten) according to above for any formation in the described technical process of this purpose, then nitride and hydrocarbon or comprise hydrocarbon and the mixture of hydrogen contacts.Therefore, utilize the only conversion of the nitride of definite part, on the surface of carbon support, formed the composition that contains carbide and nitride simultaneously.The rest part of nitride is guaranteed by maintenance condition, is incomplete from nitride to the conversion of carbide under these conditions, for example passes through restricted T _MaxOr be limited in T _MaxUnder hold-time.

In transition metal/nitrogen composition or transition metal/nitrogen/carbon composition, can believe that transition metal utilizes coordinate bond to be bonded in nitrogen-atoms.In some embodiment at least of the method for preparing catalyzer, nitrogenous compound can react with the carbon back material, and the product of this reaction further reacts to produce the wherein transition metal composition of metal-complexing on nitrogen with transition metal source compound or precursor compound.It is incidental that the reaction of nitrogenous compound and carbon back material is considered to prepare many (even not being the overwhelming majority) embodiment institute of method of transition metal composition, but can be at first carbon, the carbon and then the pyrolysis of flooding the chilled N of containing with the transition metal precursors compound by under pyrolytical condition, allowing in the presence of not the carbon back material contact, cool off then pyrolytic with nitrogenous compound to contain N in transition metal or its its source guarantee.According to this replacement scheme, in first pyrolysis step, carbon can with nitrogenous gas such as ammonia or acetonitrile greater than 700 ℃, typically contact under about 900 ℃.Second pyrolysis step can here be carried out for preparing on the carbon support under transition metal/nitrogen composition or the described temperature condition of transition metal/nitrogen/carbon composition in the presence of inertia or reducing gas (for example hydrogen and/or additional nitrogenous compound).Two pyrolysis step can be easily undertaken by allowing gas stream with suitable composition cross the fixed bed or the fluidized-bed that comprise particulate state carbon back material.

When nitrogen combines with the carbon back material, nitrogen-atoms on carbon support is typically to belong to pyridine type (pyridinic-type) by understanding, wherein nitrogen is πDian Zi of carbon contribution of carrier, for example contributes on the graphene plane of carbon, stays the unshared electron pair that is used to be coordinated on the transition metal.Further preferably, in the concentration of transition metal on the carrier not significantly greater than in order to make the saturated needed concentration of nitrogen-atoms hapto on carbon.Transiting metal concentration brought up to exceed the transition metal that this level can cause forming zeroth order (metallic forms), it is considered to for some reaction at least is non-catalytic activity.The formation from the teeth outwards of Zero-valence transition metal particle also may be induced the greying around metal particle.Though graphite itself has catalytic activity for some reaction, greying can reduce effective surface area, and this is a kind of effect (if excessive) that can damage catalyst activity.

For further being included in the modification carbon support (promptly, carbon support with the transition metal composition that forms thereon) catalyzer of the metallic active phase that upward forms, the modification carbon support with high surface area is in order to provide the high surface area that is suitable for metal deposition needed.Therefore, the modification carbon support typically has at least about 500m before the metal refining from the teeth outwards ²The Langmuir surface-area of/g.Preferably, before the metal refining, the Langmuir surface-area of modification carbon support is at least about 600m from the teeth outwards ²/ g, more preferably from about 600-800m ²/ g.Preferably, the surface-area of modified support be form from the teeth outwards carrier surface area before the transition metal composition at least about 30% and be more preferably about 40-70% of carrier surface area before forming transition metal composition on the carbon support.

The micropore surface of modification carbon support of the present invention long-pending (that is, belonging to the surface-area that diameter is lower than the hole of 20 dusts) is typically at least about 200m ²/ g more typically is about 200-400m ²/ g.Preferably, the Langmuir micropore surface of modified support is long-pending be form from the teeth outwards carrier surface area before the transition metal composition at least about 20%, 20-50% more preferably from about is more preferably the long-pending about 30-50% of Langmuir micropore surface of the carrier before forming transition metal composition on the carbon support again.

The total Langmuir mesopore of modification carbon support of the present invention and big aperture surface area (that is, belonging to the surface-area of diameter greater than the hole of 20 dusts) are typically at least about 200m ²/ g more typically is about 200-400m ²/ g.Preferably, the total Langmuir micropore of modified support and middle aperture surface area be form from the teeth outwards carrier surface area before the transition metal composition at least about 40%, be more preferably about 50-70% of the surface-area of the carrier before forming transition metal composition on the carbon support.

Modification carbon support prepared according to the methods of the invention equally preferably has is enough to allow reactant be diffused into void content in the hole of finished catalyst.Therefore, preferably, the modification carbon support that comprises transition metal/carbon composition (that is transition metal carbide) has at least about 0.50cm ³The total pore space volume of/g, more preferably at least about 0.60cm ³The void content of/g.

Except total void content, the void content of modification carbon support of the present invention distributes to preferably have and helps reactant and be diffused in the hole of finished catalyst.Preferably, it is about at the most 45% that the hole that diameter is lower than about 20 dusts has constituted the total pore space volumetrical of modification carbon support, more preferably constitutes total pore space volumetrical about at the most 30%.The total pore space volumetrical that diameter has constituted the modification carbon support greater than the hole of about 20 dusts more preferably constitutes the total pore space volumetrical at least about 65% at least about 60%.

Observe, " mesopore " (that is the hole that, has about 20-50 angstroms dia) allows reactant to be diffused into suitably in the hole of modification carbon support.Therefore, preferred mesopore has constituted the total pore space volumetrical at least about 25%, and more preferably the total pore space volumetrical is at least about 30%.Macrovoid (that is, diameter is greater than the hole of about 50 dusts) also allows reactant to be diffused into suitably in the hole of modification carbon support.Therefore, preferably these holes have constituted the total pore space volumetrical at least about 5%, and the total pore space volumetrical that has more preferably constituted catalyzer is at least about 10%.

Catalyzer of the present invention can comprise on the modification carbon support that is deposited on preparation as mentioned above, be suitable for the reaction of catalysis such as the primary alconol dehydrogenation, metallic active phase.This type of metallic activity can comprise the metal that is selected from IB family and the VIII family mutually.In various embodiments, metal is selected from copper, nickel, platinum and palladium, and wherein nickel, platinum or palladium are as the carrier of copper bearing active phase.

For the dehydrogenation of primary alconol, metallic active phase preferred package cupric.Following discussion concentrates on copper bearing catalyzer.Yet, should be realized that this discussion generally is applicable to the catalyzer that contains other metal (for example nickel, platinum and palladium).

Copper can utilize diverse ways (comprising for example electroless and metallide) to deposit on the surface of modification carbon support (that is, having formed the carbon support of transition metal composition as mentioned above from the teeth outwards).

Metallide generally comprises and allows the electric current will be by the plating bath of the metal of plating by containing of contacting with the negative electrode that comprises the modification carbon support.An alternative method of electrolytic metal plating relates to the use of " slurry electrode ", as the electrode of being described by people such as Kastening.Referring to Design of a slurry electrode reactor system, (Journal of Applied Electrochemistry (1997), 27,147-152).The plating method that uses the slurry electrode is by using metal (for example copper) anode in the slurry of modification carbon support and comprising that the slurry negative electrode of feed electrode carries out.Plating method can be by escaping into the caused copper anode of external circuit by electronics oxidation and also carrying out originally by the caused cupric ion of electronics of feed negative electrode supply.

Following discussion concentrates on electroless, because electroless is because its simplicity and low-cost but preferred technology.The electroless method by utilize with solution that the modification carbon support contacts in outside reductive agent metal ion (for example cupric ion) be reduced into metal carry out.According to the present invention, this plating bath generally comprises moisture plating medium, the water-soluble salt, reductive agent that it comprises the sedimentary metal of wanting with can with the reductive retarding agent that suppresses metal ion (for example cupric ion) before the modification carbon support contacts.This retarding agent can be that for example sequestrant is (promptly, coordination compound), it is reduced the agent reduction by forming coordination compound with want deposited metal ions so that postpone metal ion, with till the modification carbon support contacts, suppresses reduction of metal ion up to metal-salt.Plating bath can contain other composition, and these comprise for example alkaline hydrated oxide and other additive preparation, as stablizer, tensio-active agent and brightener and wetting agent.This plating bath is stable (that is, remaining abundant dispersive mixture) in the long period (for example a week or longer time) typically, and therefore the advantage that is suitable for a plurality of plating operations is provided.Typically, the pH of water-bearing media is about 7-14.

For copper, the water-soluble salt in the water-bearing media preferably is selected from cupric chloride, cupric nitrate and sulfuric acid mantoquita.In preferred embodiments, this water-soluble salt comprises copper sulfate.Although the concentration of water-soluble salt in water-bearing media is not very crucial, also prevent that simultaneously excessive precipitation, the salt concn in water-bearing media are no more than about 20 weight % typically in order to ensure sufficient metal deposition.Preferably, the salt concn in water-bearing media is about 1-10 weight %, more preferably from about 8-10 weight %.Generally, water-bearing media comprises the modification carbon support that contacts with water-bearing media of the mantoquita/every g at least about 0.2g and the modification carbon support that contacts with water-bearing media of the mantoquita that is no more than about 1.5g/every g.

Can use various reductive agents, comprise for example sodium hypophosphite (NaH ₂PO ₂), formaldehyde (CH ₂O) and other aldehyde, formic acid (HCOOH), the salt of formic acid, the salt of hydroborate (sodium borohydride (NaBH for example ₄)), the salt of the hydroborate of replacement (sodium triacetoxy borohydride (Na (CH for example ₃CO ₂) ₃BH)), sodium alkoxide, dimethyl methyl borine (DMAB) and hydrazine (H ₂NNH ₂).In preferred embodiments, reductive agent comprises formaldehyde.Reductive agent generally reduces needed stoichiometric amount according to whole or most of metal ions that will exist and is present in the water-bearing media in water-bearing media.The concentration of reductive agent in water-bearing media is no more than about 1 weight % of total plating bath typically, more typically is no more than about 0.5 weight %.

Reductive agent can be according to excessive consumption exists for the needed stoichiometry with respect to reducing at the whole or most of metal ions that exist in the water-bearing media.If excessive existence then typically exists to be no more than about 400% excessive reductant.

The suitable retarding agent (that is, sequestrant or ligand) that is incorporated in the water-bearing media of using for electroless comprises for example amino many carboxyls part, amino poly-hydroxy part, poly-hydroxy part and many carboxyls-poly-hydroxy part.Especially, this retarding agent or ligand can be selected from ethylenediamine tetraacetic acid (EDTA) (EDTA); Diethylene triaminepentaacetic acid(DTPA); N, N, N ', N '-four (2-hydroxypropyl)-quadrol; Glycerine; And tartrate.In preferred embodiments, this retarding agent comprises Seignette salt, comprises ethylenediamine tetraacetic acid (EDTA) in another embodiment.

In certain embodiments, the modification carbon support contacts with the water-bearing media of the water-soluble salt, reductive agent and the retarding agent that comprise the sedimentary metal of wanting, suppresses the reduction of metal ion (for example cupric ion) before this retarding agent can contact in the transition metal composition with the modification carbon support.Transition metal composition (for example transition metal carbide or nitride) can catalytic reduction reaction and the blockage effect that overcomes sequestrant or other retarding agent.

Along with reductive agent will be reduced into metal at the solution metal ion, metal is forming coating on the modification carbon support and/or on the surface that supports transition metal composition that forms on the part at any no transition metal on carbon support surface.Provided the mechanism of electroless below, wherein anodic reaction is the decomposition of reductive agent (as follows, formaldehyde), and cathodic reaction is the reduction of metal complexes.

Cu ²⁺+1/2e ---＞Cu ⁰

Observe, the reductive agent that comprises formaldehyde more effectively plays a role in alkaline environment.This is because formaldehyde is present in the water-bearing media as methylene glycol.The existence of basic component can promote the deprotonation of methylene glycol; Therefore, water-bearing media typically also comprises basic component.Typically, the concentration of basic component in water-bearing media is at least about 0.1 weight %.Preferably, the concentration of basic component in water-bearing media is about 0.5-5 weight %.1-3 weight % more preferably from about.

When water-bearing media comprises basic component, must carefully avoid sedimentary formation, sedimentary formation is caused by positively charged ion and the reaction between the hydroxide ion at the sedimentary metal of want.Preferably should avoid precipitation, because formed any throw out can consume the metal that is deposited in addition on the carbon support; The nonactive throw out of catalysis (Cu (OH) for example ₂) also can be deposited on the surface of modified support.This type of precipitation can prevent the intrapore deposition of transition metal at carbon support.The existence that suppresses metal ion (for example cupric ion) reductive retarding agent before contacting in the transition metal composition with the modification carbon support generally suppresses this precipitation fully.Therefore, the basic component in water-bearing media does not influence plating technic.

The electroless deposition of metal on the transition metal composition that supports may be carried out too soon in some cases, therefore prevent that metal is diffused in the carbon structure (promptly fully, metal is diffused in the hole of carbon support fully), and correspondingly prevent the uniform deposition of metal on carbon-supported transition metal composition.The speed of plating is directly proportional with plating temperature; Therefore, a kind of approach of control plating rate is the control plating temperature.Have been found that, operation plating process can be improved the diffusion that the sedimentary metal of wanting enters into the hole of the transition metal composition (for example carbide, nitride or carbide-nitride) that supports under moderate temperature, therefore improves the homogeneity of metal deposition.Therefore, this plating be typically about 1-50 ℃, more typically carry out (that is, the modification carbon support contacts with water-bearing media) under about 2-25 ℃ the temperature.Typically, the modification carbon support contacted with water-bearing media at least about 0.5 hour, more typically was about 0.5-3 hour.

Although being plated on the transition metal composition surface, copper can easily carry out, but unfortunately, the part of transition metal will be removed or lixiviate transition metal/nitrogen, transition metal/carbon or the transition metal/carbon/nitrogen composition from carbon support in the plating process.

Transition metal can be deposited on the ion institute oxidation of the metal on the transition metal composition owing to the needs that transition metal composition (that is, nitride, carbide-nitride or carbide) is existed in water-bearing media/plating bath from the lixiviate on the carrier surface.For example, oxidized carbide is unsettled, and therefore, when the transition metal composites comprised the transition metal carbide of enough ratios, transition metal more may be from lixiviate on the surface of carbon support.For the instable explanation of oxidized carbide is that it causes that the oxidation of transition metal and it removes from oxide matrix.The oxidation of nitride, carbide-nitride or carbide is directly proportional with plating temperature; Therefore, this problem generally can according to above for plating temperature given pass at low temperatures that plating solves through discussion.Because the caused transition metal lixiviate of oxidation of carbide or nitride also can partly be controlled by the existence of reductive agent, reductive agent helps the surface of transition metal carbide or nitride is remained under the abundant reductive state.

Except control and/or the lixiviate of minimizing transition metal, the oxidation that prevents carbide or nitride also is favourable, because metal generally can not be plated on the already oxidised carbide or nitride, or, if its complete plating can not be created in stable metallographic phase under reaction (for example dehydrogenation) condition.This be considered at least in part owing between already oxidised carbide and copper than weak interaction.

As described, retarding agent be present in the water-bearing media in case with the metallic contact of want plating before prevent reduction of metal ion and when retarding agent was sequestrant, it formed coordination compound by the metal with want plating and brings into play this function.Typically, the concentration of retarding agent in water-bearing media is at least about 3 weight %.Preferably, the concentration of retarding agent in water-bearing media is about 3-6 weight %.Yet if too the retarding agent of vast scale is present in the water-bearing media, owing to form coordination compound between retarding agent and transition metal, transition metal can be from lixiviate on the surface of carbon support.

The preferred proportion of the retarding agent that therefore, exists in water-bearing media also depends on the concentration of the metal-salt that exists in water-bearing media.The ratio that has been found that these components of control helps to obtain best plating factor.That is to say that the metal that comprises the enough parts of sufficient to guarantee is kept retarding agent concentration to be lower than that concentration that meeting as discussed above causes lixiviate by the retarding agent of that consumption of plating simultaneously.According to the present invention, the mole number of retarding agent is at least about 1: 1 with the molar ratio of the mole number of the metal that exists in water-bearing media, typically at least about 1.5: 1, more typically at least about 2.0: 1, more more typically at least about 2.5: 1.Yet the mole number of retarding agent preferably is no more than about 3: 1 with the molar ratio of the mole number of the metal that exists in water-bearing media, thereby avoids the formation of excessive coordination compound between retarding agent and transition metal.

Except plating temperature and retarding agent concentration, the mode that one or more in the component are introduced in the water-bearing media can be improved, with control plating rate and the lixiviate from the carrier surface.Fig. 1 is the SEM image that has deposited the carbon-supported molybdenum carbide of copper according to the aforesaid method that wherein just has reductive agent when electroless begins from the teeth outwards.As shown in fig. 1, observe, for the situation of carbon-supported molybdenum carbide, will cause considerable metal cluster formation and in the carbon support hole, be lower than desirable plating according to the plating that wherein when electroless begins, carries out with regard to the aforesaid method that has reductive agent.Yet this method causes few transition metal lixiviate.

Have been found that, for example, the modification carbon support with reductive agent is incorporated into after the water-bearing media that comprises metal-salt and retarding agent contacts water-bearing media can be so that the sedimentary metal of wanting be diffused in the hole of carbon support more because utilize the caused delayed action of the introducing of the reductive agent plating rate that slowed down; Therefore compare with viewed effect when when the modification carbon support contacts with water-bearing media, having reductive agent, cause more even metal deposition.

Fig. 2 is the SEM image that deposits the carbon-supported molybdenum carbide of copper according to this method (that is, postpone the introducing of reductive agent, until carrier with till water-bearing media contacts) from the teeth outwards.As shown in Figure 2, use this method, observe at the intrapore uniform copper facing of carbon support (that is, do not have to form in a large number copper bunch) and enough plating.On the other hand, modified support is incorporated in the presence of not at reductive agent and can causes in the water-bearing media because the height transition metal lixiviate from the carrier surface that the oxidation of carbide or nitride surface causes, this is owing to the unstable of oxidized carbide and nitride.For example, observe molybdenum lixiviate up to 20% for copper-plated carbon-supported molybdenum carbide shown in figure 2.

Also considered with after the water-bearing media that comprises reductive agent and retarding agent contacts metal-salt to be incorporated in the water-bearing media at the modification carbon support.The plating that carries out provides by the caused lixiviate of the oxidation of carbide or nitride and has reduced (for example hanging down the transition metal that forms to 5% on carbon support) in such a way, and this is to keep fully reduction because carbide or nitride surface have been guaranteed in the existence of reductive agent.Yet plating carries out too soon, and this is because exist overall stoichiometric reductive agent and salt when carbon support contacts with water-bearing media at first.Fig. 3 be according to this method (that is, the modification carbon support with postpone metal-salt after water-bearing media contacts and be incorporated in the water-bearing media) deposit the TEM image of the carbon-supported molybdenum carbide of copper from the teeth outwards.As shown in Figure 3, this method can't be provided at the intrapore uniform distribution of carbon support (that is, occur considerable copper bunch) or inadequate plating.Therefore, reduced lixiviate even compare with above-mentioned those methods, this method (although being acceptable in some cases) is not preferred.Metal deposition according to this replacement scheme does not resemble using the deposition that is realized when wherein the part of reductive agent is introduced the aforesaid method that is delayed even usually.

Therefore, preferably, all can solve by controlling the mode that each component and modification carbon support be introduced in the water-bearing media for the consideration of the usually conflict of the oxidation of plating rate (it directly influences the homogeneity and the quality of plating) and carbide or nitride.

Also studied when carrier is initial and contact with water-bearing media and follow at carrier when additional reductive agent being incorporated into water-bearing media solution after water-bearing media contacts, reductive agent is present in the water-bearing media to compare the lower consumption of the needed consumption of metal that metal ion is reduced into the plating of being wanted on stoichiometry.Along with the copper metal deposition on carrier, slurry can stir.A part that postpones reductive agent in this way is incorporated in the water-bearing media so that form the elementary electroless slurry that comprises the reductive agent that is lower than the stoichiometry aequum, can reduce plating rate, therefore make that the sedimentary metal of wanting is diffused in the hole of carbon support more, cause more even metal deposition.The reductive agent of initial portion is enough to the reducing metal ion, also is enough to provide abundant reductive carbide or nitride surface to control by the caused lixiviate of the oxidation of carbide and nitride surface simultaneously.Fig. 4 is the SEM image that deposits the carbon-supported molybdenum carbide of copper according to this method (that is, postpone the introducing of a part of reductive agent, until carrier with till water-bearing media contacts) from the teeth outwards.As shown in Figure 4, use this method to realize the uniform deposition of copper.In addition, low molybdenum lixiviate (for example about at the most 5 weight %) has taken place in this method.In certain embodiments, this electroless slurry comprise be no more than stoichiometric amount about 2% for the metal ion of want plating being reduced needed reductive agent, and in other embodiments the electroless slurry comprise stoichiometric amount about 2-10% be that metal ion with want plating reduces needed reductive agent.

Postponing a part of reductive agent is incorporated into and also the decomposition of reductive agent can be reduced to minimum in the water-bearing media.For example for the reductive agent that comprises formaldehyde, the reaction that it resolves into hydrogen is delayed.

Though above-mentioned each method has realized the metal deposition on carbide or nitride surface, but preferable methods is the method that the introducing of wherein a part of reductive agent is delayed, and solves because two factors of this of the oxidation of plating rate and carbide or nitride all obtain fullest ground.As previously discussed, plating temperature is preferred for controlling plating rate, and therefore the even metal deposition is provided.Therefore, the beneficial effect that further preferably will hang down plating temperature with postpone the method that a part of reductive agent is incorporated in the water-bearing media and combine.Therefore, in preferred embodiments, this plating temperature is no more than about 2 ℃, and is no more than to needed about 5% the reductive agent by stoichiometric amount of the metal ion of want plating reduction is introduced in and forms the electroless slurry in the water-bearing media.Yet in various embodiments, plating temperature can be about 1-20 ℃, about 1-10 ℃ or about 1-5 ℃.

Metal is till the pH that the plating on the modification carbon support generally proceeds to water-bearing media reaches predetermined pH, based on the consumption of hydroxide ion.Therefore, the speed of pH decline directly relates to plating rate and therefore is controlled in based in the above-mentioned OK range for the described Consideration of control plating process.Typically, plating is to be that about 13 water-bearing media begins with pH, and is to interrupt in about 8 o'clock at the pH of water-bearing media typically.According on regard to the described method of plating rate (for example temperature of reductive agent and introducing), the speed that preferred pH descends is no more than about 0.5/ minute.

Based on foregoing, several factors influences the plating operation as can be seen.Metal, retarding agent, reductive agent and the hydroxide composition concentration in water-bearing media for example.Therefore, preferably these components concentration separately remains in the OK range.

For dehydrogenation catalyst of the present invention, be deposited on metal typical ground on the modification carbon support constituted catalyzer at least about 5 weight %.Preferably, be deposited on about 5-30 weight % of the metal formation catalyzer on the modification carbon support, more preferably constitute about 15-25 weight % of catalyzer, more preferably constitute about 18-23 weight % of catalyzer again.Catalyzer comprises in the embodiment that is deposited over the copper on the modification carbon support therein, and this catalyzer typically comprises the copper at least about 10 weight %, more typically at least about the copper of 15 weight %.Preferably, catalyzer comprises the copper of about 10-30 weight %, the copper of 15-25 weight % more preferably from about, the copper of 18-23 weight % more preferably from about again.In certain embodiments, preferably, described copper bearing catalyzer comprises the sedimentary as stated above precious metal (for example platinum) that is no more than about 3 weight %, more preferably no more than the precious metal of about 1 weight %, again more preferably no more than the precious metal of about 0.5 weight %.In other embodiments, preferred copper bearing catalyzer of the present invention comprises the nickel that is no more than about 1 weight %, more preferably no more than the nickel of about 1 weight %, again more preferably no more than the nickel of about 0.5 weight %.

The oxide catalyst of the present invention that is included in the transition metal composition that forms on the carbon support can further comprise the active phase that contains precious metal.The catalyzer that comprises the active phase that contains precious metal is effectively for the oxidation of tertiary amine (for example N-((phosphonomethyl)) iminodiethanoic acid), and also is effective for the oxidized byproduct (for example formaldehyde and formic acid) of this reaction.Comprise in the embodiment of the precious metal (for example platinum) that is deposited on the modification carbon support at catalyzer of the present invention, this precious metal typically deposits according to well-known method.These methods comprise for example liquid phase process, for example reactive deposition technology (for example via the deposition that reduction realized of precious metal chemical complex with via the deposition that hydrolysis realized of precious metal chemical complex), ion exchange technique, excess solution dipping and incipient wetness impregnation; Vapor-phase process, for example physical deposition and electroless plating; Precipitation; And electrochemical displacement deposition method, for example electroless deposition and electrolytic deposition.

Preferably, precious metal deposits to via dipping method on the surface of modification carbon support, and this method comprises allows the modification carbon support contact with the solution of the salt that comprises the sedimentary precious metal of wanting, and carries out the hydrolysis of salt subsequently.Generally, the salt of the sedimentary precious metal of is selected from hydrogen, sodium, potassium and ammonium salt.Also comparatively cheap, be applicable to that an example of the platinum salt in the solution deposition is chloroplatinic acid (H ₂PtCl ₆).

Also can use to comprise to be in its more solution of the salt of the precious metal under a kind of state among the suboxide state, with noble metal loading on the surface of modification carbon support.For example replace to use the salt (H for example of Pt (IV) ₂PtCl ₆), can use the salt of Pt (II).In another embodiment, use the platinum (for example colloidal state platinum) that is in elementary state.Use these more the metal precursor of lower valency can cause the less oxidation of modification carbon support, therefore, when noble metal loading is from the teeth outwards, on the surface of carrier, form less oxygen-containing functional group.An example of Pt (II) salt is K ₂PtCl ₄Pt (II) salt of another kind of potentially useful is diamines two oxynitroso platinum (II).

The appropriate method of noble metal loading is at US patent No.6, discusses in 417,133, and their whole disclosures are introduced into for reference.

For oxide catalyst of the present invention, platinum typically with catalyzer at least about 0.5 weight %, more typically be that the ratio at least about 1 weight % with catalyzer exists.Preferably, platinum is to be equivalent to about 1-10 weight % of catalyzer, more preferably to be equivalent to about 2-8 weight % of catalyzer, more preferably to be equivalent to the ratio existence of about 2-5 weight % of catalyzer again.

Except that precious metal, can on the surface of carbon support, there be at least a promotor.Though this promotor typically deposits on the surface of carbon support, can use other source (for example carbon support itself can contain promotor naturally) of promotor.Promotor tending to improved catalyst selectivity, activity and/or stable.Promotor can be reduced the lixiviate of precious metal in addition.

Promotor can for example be at the lip-deep additional precious metal of carbon support.For example have been found that ruthenium and palladium can comprise on the catalyzer that is deposited on the lip-deep platinum of carbon support as promotor a kind of.This promotor or can be for example to be selected from following metal: tin (Sn), cadmium (Cd), magnesium (Mg), manganese (Mn), nickel (Ni), aluminium (Al), cobalt (Co), bismuth (Bi), plumbous (Pb), titanium (Ti), antimony (Sb), selenium (Se), iron (Fe), rhenium (Re), zinc (Zn), cerium (Ce) and zirconium (Zr).Preferably, this promotor is selected from bismuth, iron, tin and titanium.In particularly preferred embodiments, this promotor is tin.In another particularly preferred embodiment, this promotor is iron.In additional preferred embodiment, this promotor is titanium.In another particularly preferred embodiment, this catalyzer comprises iron and tin simultaneously.Iron, tin or the two use general (1) reduce precious metal lixiviate and (2) of the catalyzer that uses and tend to improve and/or keep activity of such catalysts when catalyzer are used to carry out the oxidation of PMIDA in several cycles.It generally is most preferred wrapping ferruginous catalyzer, because they tend to have maximum activity and stable for the oxidation of formaldehyde and formic acid.

In a preferred embodiment, promotor is easier to be more oxidized than precious metal.If promotor has first ionizing potential lower than precious metal, then it " easier to be oxidized ".First ionizing potential of element is commonly known in the art, and can (Boca Raton finds in Florida) for CRC Press, Inc. at for example CRC Handbook of Chemistryand Physics.

Amount (no matter whether relevant with carbon surface itself, metal or their mixture) the lip-deep promotor of carbon support can change in wide region, and this depends on for example employed precious metal and promotor.Typically, the weight percentage of promotor is at least about 0.05% ([total mass of the quality ÷ catalyzer of promotor] * 100%).The preferably about 0.05-10% of the weight % of promotor, 0.1-10% more preferably from about, more preferably from about 0.1-2%, most preferably from about 0.2-1.5% again.When promotor was tin, this weight percentage most preferably was about 0.5-1.5%.Be lower than 0.05% promotor weight percentage and generally can not promote activity of such catalysts in long-time.On the other hand, tend to reduce activity of such catalysts greater than about 10% weight percentage.

The molar ratio of precious metal and promotor also can change in wide region, and this depends on for example employed precious metal and promotor.Preferably, this ratio is about 1000: 1 to about 0.01: 1; More preferably from about 150: 1 to about 0.05: 1; More preferably from about 50: 1 to about 0.05: 1 again; Most preferably from about 10: 1 to about 0.05: 1.For example, the catalyzer that comprises platinum and iron preferably has about 3: 1 platinum and the molar ratio of iron.

In certain embodiments, alloying takes place and forms the alloyed metal (AM) particle with at least a promotor (for example tin or iron) in precious metal (for example platinum).

For the carbon support that has formed transition metal composition thereon (being the modification carbon support), the feature of surface-area that meeting influence can supply copper, precious metal or other metal active to deposit the transition metal composition of usefulness mutually be transition metal composition for some condition (for example basic metal plating condition and with to be plated on this modification carbon support on the positively charged ion of metal between contact) under by the resistibility of removing from the carbon support surface.Therefore, preferably, when contacting at least about 3 hours with alkaline aqueous plating medium under basic metal plating condition, the transition metal composition of the present invention that is no more than about 20 weight % is removed from the surface of carbon support.In addition preferably, when be deposited on the modification carbon support on the positively charged ion of metal when contacting at least about 3 hours, the transition metal composition of the present invention that is no more than about 5 weight % is removed from the surface of carbon support.

Generally, oxide catalyst of the present invention preferably has high surface area.The formation of transition metal/nitrogen, transition metal/carbon or transition metal/carbon/nitrogen composition is typically relevant with some minimizings of Langmuir surface-area.The loss of surface-area is the result that carbon surface is applied by the transition metal composition (for example amorphous membrance of transition metal composition and/or larger particles form) than low surface area.Unbodied transition metal composition can be the form of amorphous granular or amorphous membrance.Preferably, the loss of surface-area is not more than about 40%.When forming transition metal composition under above-described optimum condition, the loss of total Langmuir surface-area is typically between about 20-40%.Therefore, general, the surface-area of catalyzer be form from the teeth outwards the carbon support before the transition metal composition surface-area at least about 60%, more generally be about 60-80%.

Typically, this catalyzer has at least about 500m ²/ g, more typically at least about 600m ²Total Langmuir surface-area of/g.Preferably, total Langmuir surface-area of catalyzer is at least about 800m ²/ g is more preferably at least about 900m ²/ g.Generally preferably, after transition metal composition formed, total Langmuir surface-area of catalyzer kept at least about 1000m ²/ g, more preferably at least about 1100m ²/ g even more preferably at least about 1200m ²The value of/g.Generally, this catalyzer has about 600-1500m ²/ g, about 600-1400m typically ²Total Langmuir surface-area of/g.In certain embodiments, catalyzer has about 800-1200m ²Total Langmuir surface-area of/g.Preferably, catalyzer has about 1000-1400m ²/ g, 1100-1400m more preferably from about ²/ g even 1200-1400m more preferably from about ²Total Langmuir surface-area of/g.

When forming transition metal composition according to preferable methods, can believe, composition comprises the very thin particle of suitable vast scale, for example wherein at least about the transition metal of 20 weight % be unbodied form or less than 15nm, more typically less than 5nm, more typically less than the particle form of 2nm, measure according to X-ray diffraction method.

Further preferably, compare with carbon support, micropore Langmuir surface-area has reduced and has been no more than 45%, more preferably no more than about 40%.Therefore, the micropore Langmuir surface-area of oxide catalyst generally be form from the teeth outwards the carbon support before the transition metal composition micropore Langmuir surface-area at least about 55%, more generally at least about 60%, more more generally at least about 80%.Typically, the micropore Langmuir surface-area of catalyzer is the about 55-80% that forms the micropore Langmuir surface-area of transition metal composition carbon support before from the teeth outwards, and more typically about 60-80% more typically is about 70-80% again.

The Langmuir surface-area of oxide catalyst of the present invention that belongs to the hole (being micropore) that diameter is lower than 20 dusts is typically at least about 750m ²/ g, more typically 800m at least ²/ g is more more typically at least about 800m ²/ g, even more typically be at least about 900m ²/ g.Preferably, the micropore Langmuir surface-area of oxide catalyst is about 750-1100m ²/ g, more preferably from about 750-1000m ²/ g.

Except the long-pending preferred minimizing of micropore surface, further preferably owing on carbon support, form transition metal composition, the mesopore of total and macropore Langmuir surface-area reduced be no more than about 30%, more preferably no more than about 20%.Therefore, general, the total mesopore of oxide catalyst and macropore Langmuir surface-area generally be form from the teeth outwards the total mesopore of the carbon support before the transition metal composition and macropore Langmuir surface-area at least about 70%, more generally be at least about 80%.Typically, the total mesopore of catalyzer and macropore Langmuir surface-area are to form the total mesopore of transition metal composition carbon support before and about 70-90% of macropore Langmuir surface-area from the teeth outwards.

Generally, the mesopore of total and big aperture surface area are at least about 175m ²/ g more generally is 200m at least ²/ g.Preferably, the total mesopore of oxide catalyst and macropore Langmuir surface-area are about 175-300m ²/ g and 200-300m more preferably from about ²/ g.In certain embodiments, the mesopore of total and big aperture surface area are about 175-250m ²/ g.

In addition or as an alternative, preferably, the micropore Langmuir surface-area of catalyzer keeps at least about 750m ²/ g, more preferably at least about 800m ²The value of/g and after transition metal composition forms the total mesopore and the macropore Langmuir surface-area of catalyzer remain at least about 175m ²/ g, more preferably at least about 200m ²The value of/g.

In various particularly preferred embodiments of the present invention, the X-ray diffraction analysis that is in the limit of detection of 1nm does not detect the transition metal composition particle of any major part.Therefore, be believed that at present the transition metal composition particle is to be present on the surface of carbon support or to be present in the amorphous film form on the surface of carbon support with the discrete particles form less than the 1nm granularity.Yet, the basis that is reduced to surface-area after the formation transition metal composition on carbon support, infer that reasonably this transition metal composition can exist as amorphous film at least in part, because will expect the increase of surface-area less than the sedimentary situation of the crystal grain of 1nm for granularity.

Equally preferably, dehydrogenation catalyst of the present invention (that is, having deposited the modification carbon support of metallic active phase) has high surface area.Typically, this catalyzer has at least about 500m ²/ g, more typically at least about 600m ²/ g and more typically about again 500-1200m ²The Langmuir surface-area of/g.Generally, this catalyzer has about 600-1000m ²/ g and more generally about 600-800m ²The Langmuir surface-area of/g.

Other favourable feature of oxidation of the present invention and dehydrogenation catalyst is to be enough to allow reactant be diffused into void content in the catalyst pores.Therefore, preferred, the catalyzer of the present invention that is included in the transition metal composition that forms on the carbon support typically has at least about 0.1cm ³/ g and more typically at least about 0.5cm ³The void content of/g.Generally, this type of catalyzer has about 0.1-2cm ³/ g and more generally about 0.5-1.5cm ³The void content of/g.

Except the volume of total pore space, the void content of oxidation of the present invention and dehydrogenation catalyst distributes to preferably have and helps reactant and be diffused in the hole of finished catalyst.Preferably, it is no more than about 45% that the hole that diameter is lower than about 20 dusts accounts for catalyzer total pore space volumetrical, more preferably accounts for total pore space volumetrical no more than about 30%.The total pore space volumetrical that diameter preferably accounts for catalyzer greater than the hole of about 20 dusts more preferably accounts for the total pore space volumetrical at least about 65% at least about 60%.

Observing " mesopore " (that is, diameter is the hole of about 20-40 dust) allows reactant to be diffused into suitably in the hole of catalyzer.Therefore, preferred mesopore has constituted the total pore space volumetrical at least about 25%, more preferably constitutes the total pore space volumetrical at least about 30%.Macropore (that is, diameter is greater than the hole of about 40 dusts) also allows reactant to be diffused into suitably in the hole of catalyzer.Therefore, preferred, these holes have constituted the total pore space volumetrical at least about 5%, have more preferably constituted catalyzer total pore space volumetrical at least about 10%.

Generally preferably, transition metal composition (for example transition metal carbide or transition metal nitride) is evenly distributed on the surface of pore wall and (that is all surfaces that can arrive with the catalyzer fluid in contact) between the crack of granules of catalyst on the passage basically.The granularity of the transition metal composition of being measured by X-ray diffraction method for example can influence this uniform distribution, and it is more little to have observed the particulate state crystalline size of transition metal composition, and its deposition is even more.

For the oxide catalyst of the present invention that comprises the transition metal composition that is deposited on the carbon support, general, the transition metal composition particulate has the granularity that is lower than about 1000nm at least about 95 weight %, by their overall dimension.Typically, the transition metal composition particulate has the granularity that is lower than about 250nm at least about 80 weight %, by their overall dimension.More typically, the transition metal composition particulate has the granularity that is lower than about 200nm at least about 70 weight %, by their overall dimension.Again more typically, has the granularity that is lower than about 18nm at least about this transition metal composition particle of 60 weight %, by their overall dimension.Even more typically, at least about 20 weight %, preferably this transition metal composition particle at least about 55 weight % has the granularity that is lower than about 15nm, by their overall dimension.Preferably, have at least about this transition metal composition particle of 20 weight % and to be lower than about 5nm, more preferably less than about 2nm with even more preferably less than the granularity of about 1nm, by their overall dimension.More preferably, this transition metal composition particle of about 20-95 weight % has the granularity that is lower than about 1nm, and 20-100 weight % more preferably from about is by their overall dimension.

Generally, has the granularity that is lower than about 1000nm by quantity at least about this transition metal composition particle of 75%, by their overall dimension.Typically, has the granularity that is lower than about 250nm by quantity at least about this transition metal composition particle of 60%, by their overall dimension.More typically, has the granularity that is lower than about 200nm by quantity at least about this transition metal composition particle of 50%, by their overall dimension.Again more typically, has the granularity that is lower than about 18nm by quantity at least about this transition metal composition particle of 40%, by their overall dimension.Even more typically, has the granularity that is lower than about 15nm by quantity at least about 35% transition metal composition particle, by their overall dimension.

For the dehydrogenation catalyst that comprises the active phase of containing metal (for example cupric) that is deposited on the modification carbon support (it is included in the transition metal composition that comprises molybdenum or tungsten that forms on the carbon support), typically, the particulate of the transition metal composition that forms on carbon support demonstrates the granularity that is lower than about 100nm at least about 99%, therefore help the uniform distribution of transition metal composition on whole carbon support, because observed the particle with this size of vast scale more can provide transition metal composition on carbon support uniform coating.The granularity at least about the about 5-50nm of 95% demonstration of carbide that more preferably, on carbon support, forms or nitride particles.

Having observed the uniform distribution of transition metal composition on carbon support (that is, the gathering cluster of transition metal reduces and/or the suitable distribution of transition metal composition in the carbon support hole) can improve the catalytic activity that comprises the catalyzer that is deposited on the transition metal composition on the carbon support and/or can allow metallic active improvement on the modification carbon support to apply for the situation of dehydrogenation catalyst.

Fig. 5 is high resolution transmission electron microscope (HRTEM) photo of the prepared carbon-supported molybdenum carbide of the aforesaid method that exists with 15 weight % ratios according to molybdenum carbide wherein.As shown in, show the uniform distribution of molybdenum carbide on whole carbon support according to the carbon support that is formed with molybdenum carbide thereon of method for preparing.

Fig. 6 is scanning electron microscope (SEM) photo of the prepared carbon-supported molybdenum carbide of the aforesaid method that exists with 10 weight % ratios according to carbide wherein.As shown in, show the uniform distribution of molybdenum on whole carbon support according to aforesaid method with the carbon support that 10 weight % ratios of modification carbon support are formed with molybdenum carbide thereon.Fig. 7 is transmission electron microscope (TEM) photo of the prepared carbon-supported molybdenum carbide of the aforesaid method that exists with 10 weight % ratios according to carbide wherein.As shown in, the carbon support that is formed with molybdenum carbide thereon with 10 weight % ratios of modification carbon support according to aforesaid method shows the homogeneity of molybdenum carbide population distribution, this is considered at least in part the size-grade distribution owing to molybdenum carbide.

Uniform distribution can recently be represented by the percentage of the carbon support surface-area that is covered by transition metal composition.(transition metal composition that for example comprises the carbide or the nitride of molybdenum or tungsten) preferably in certain embodiments, the suitable part of carbon support surface-area is applied by transition metal composition.Generally, at least about 20%, more generally applied by transition metal composition (for example transition metal carbide or nitride) at least about 50% carbon support surface-area.Typically, about 20-80% and more typically the carbon support surface-area of about 50-80% applied by transition metal composition (for example transition metal carbide or nitride).

Oxide catalyst of the present invention can demonstrate one or more at people's such as Ebner US patent No.6, the performance of describing in 417,133, and its whole disclosures are hereby incorporated by reference.These features can be gone to the 7th hurdle the 23rd at for example the 3rd hurdle the 6th row; The 8th hurdle the 27th row is to the 9th hurdle the 24th row; The 10th hurdle 53-57 is capable; The 11st hurdle the 49th row is to the 14th hurdle the 18th row; The 14th hurdle the 50th row is to the 16th hurdle the 3rd row; The 17th hurdle the 14th row is to the 21st hurdle the 2nd row; The 26th hurdle (embodiment 2); The 27th hurdle 21-34 capable (embodiment 4); Find in the 40th hurdle the 61st row (embodiment 7-19) with the 30th hurdle the 21st row.

Oxide catalyst of the present invention can be included in the lip-deep carbon nanotube of carbon support, and this carbon support can contain a certain proportion of transition metal that is included in the catalyzer.In addition or as an alternative, this carbon nanotube can contain a part of nitrogen of transition metal composition.Typically, any this type of transition metal is present in the root or the top of nanotube, yet transition metal also can exist on the length of nanotube.Carbon nanotube typically has the diameter at least about 0.01 μ m, more typically has the diameter at least about 0.1 μ m.In certain embodiments, this carbon nanotube has the diameter that is lower than about 1 μ m, has the diameter that is lower than about 0.5 μ m in other embodiments.

Some example of above-mentioned catalyzer (for example comprise the catalyzer that is deposited on the transition metal composition on the carbon support and further comprise this type of catalyzer of precious metal) can be used for liquid phase oxidation reaction.The example of this type of reaction comprises alcohols and the oxidized formation aldehyde of polyvalent alcohol, ketone and acid (the oxidized formation Glycerose of for example oxidized formation acetone of 2-propyl alcohol, and glycerine, Protosol or R-Glyceric acid); The oxidized formation acid of aldehyde (the oxidized formation pyromucic acid of for example oxidized formation formic acid of formaldehyde, and furfural); The oxidized formation secondary amine of tertiary amine (the oxidized formation iminodiethanoic acid of nitrilotriacetic acid(NTA) (" NTA ") (" IDA ") for example; The oxidized formation primary amine of secondary amine (for example oxidized formation glycine of IDA); With various acid (for example formic acid or acetate) oxidized formation carbonic acid gas and water.

Disclosed here oxidation catalysis immunomodulator compounds is particularly suitable for the catalytic tertiary amine liquid-phase oxidation and becomes secondary amine, for example in the preparation of glyphosate and related compound and derivative.For example the tertiary amine base material can be corresponding to the compound of the general formula I I with following structure:

[general formula I I]

R wherein ¹Be selected from R ⁵OC (O) CH ₂-and R ⁵OCH ₂CH ₂-, R ²Be selected from R ⁵OC (O) CH ₂-, R ⁵OCH ₂CH ₂-, the alkyl of alkyl, replacement, acyl group ,-CHR ⁶PO ₃R ⁷R ⁸With-CHR ⁹SO ₃R ¹⁰, R ⁶, R ⁹And R ¹¹Be selected from hydrogen, alkyl, halogen and-NO ₂, and R ³, R ⁴, R ⁵, R ⁷, R ⁸And R ¹⁰Be selected from the alkyl and the metal ion of hydrogen, alkyl, replacement.Preferably, R ¹Comprise R ⁵OC (O) CH ₂-, R ¹¹Be hydrogen, R ⁵Be selected from hydrogen and agricultural upward acceptable positively charged ion and R ²Be selected from R ⁵OC (O) CH ₂-, the alkyl of acyl group, alkyl and replacement.As mentioned above, oxide catalyst of the present invention is particularly suitable for the oxidized cracking of catalysis PMIDA substrate such as N-((phosphonomethyl)) iminodiethanoic acid or its salt and forms N-((phosphonomethyl)) glycine or its salt.In this type of embodiment, catalyzer can be effectively with by product oxidation of formaldehyde formic acid, carbonic acid gas and/or water.

Above-mentioned catalyzer especially is used in and is lower than under 7 the pH level and especially at the liquid phase oxidation reaction that is lower than under 3 the pH level.A kind of this type of reaction is PMIDA or its salt oxidized formation N-((phosphonomethyl)) glycine or its salt in the environment of the pH of about 1-2 level.This reaction usually is to carry out in the presence of the solvent that can dissolve precious metal, and in addition, reactant, intermediate or product usually dissolve precious metal.Some catalyzer of the present invention is owing to not existing precious metal to avoid these problems.Yet, advantageously, have been found that the catalyzer of the present invention that contains precious metal is useful in this type of environment.

Following narration discloses the transition metal composition (for example transition metal nitride, transition metal carbide or transition metal carbide-nitride) that contains as catalyzer especially or the above-mentioned catalyzer that further contains the noble metal active phase is used to carry out oxidative cracking reaction formation N-((phosphonomethyl)) glycine of PMIDA or its salt or the purposes of its salt.Yet, will be appreciated that following public principle generally is applicable to other liquid phase oxidation reaction, especially be lower than those reactions under 7 the pH level and involving those reactions of solvent, reactant, intermediate or the product that can dissolve precious metal.

In order to begin the PMIDA oxidizing reaction, preferably exist and add PMIDA reagent (that is, PMIDA or its salt), catalyzer and solvent in the downhill reaction device at oxygen.Solvent most preferably is a water, but other solvent (for example Glacial acetic acid) is suitable equally.

Reaction can be carried out in various intermittences, semi-batch and flow reactor system.The configuration of reactor is not crucial.Suitable common response device configuration comprises for example stirred autoclave, fixed-bed reactor, trickle-bed reactor, fluidized-bed reactor, burble reactor, plug flow reactor and parallel flow reactor.

When carrying out in the flow reactor system, the residence time in reaction zone can change in wide region, and this depends on employed concrete catalyzer and condition.Typically, this residence time can change in about 3-120 minute scope.Preferably, this residence time is about 5-90 minute, more preferably from about 5-60 minute.When carrying out in batch reactor, the reaction times typically changes in about 15-120 minute scope.Preferably, the reaction times is about 20-90 minute, more preferably from about 30-60 minute.

In a broad sense, oxidizing reaction can be according to the present invention under the wide temperature range and be lower than atmosphere and be pressed onto to be higher than under the atmospheric pressure and carry out.The use of mild conditions (for example room temperature and barometric point) has tangible industrial advantage, because can use the equipment of less expensive.Yet, operate with being higher than under the normal atmosphere at comparatively high temps, increase capital requirements simultaneously, tend to improve the phase transition between liquid and gas and improve the PMIDA oxidizing reaction rate.

Preferably, PMIDA reaction is under about 20-180 ℃ temperature, more preferably from about 50-140 ℃ and most preferably from about carry out under 80-110 ℃ the temperature.Be higher than under about 180 ℃ temperature, starting material tend to beginning and decompose at leisure.

Employed pressure generally depends on employed temperature in the PMIDA oxidising process.Preferably, pressure is enough to prevent the reaction mixture boiling.If oxygen-containing gas is as oxygen source, then pressure is enough to preferably also cause that oxygen is dissolved in the reaction mixture with certain speed, and this speed is enough to make that the PMIDA oxidation can be not restricted because of insufficient oxygen supply.This pressure preferably equals barometric point at least.More preferably, pressure is about 30-500 pound/square inch, most preferably from about 30-130 pound/square inch.

The preferably about 0.1-10 weight of this catalyst concn % ([the quality ÷ total reactant quality of catalyzer] * 100%).More preferably, the preferably about 0.1-5 weight of this catalyst concn %, more preferably from about 0.2-5 weight % and most preferably from about 0.3-1.5 weight % again.Concentration greater than about 10 weight % is difficult to filter.On the other hand, the concentration that is lower than about 0.1 weight % tends to produce unacceptable low reaction speed.

The invention further relates to a kind of catalyst system, its comprise transition metal composition/C catalyst of the present invention (preferably being substantially free of the noble metal active phase) with at people's such as Ebner US patent No.6,417, the dual functional catalyst of describing in 133 that contains precious metal (promptly, energy oxidation PMIDA and the further simultaneously catalyzer of realizing the oxidation of formaldehyde and formic acid by product), the whole disclosure of this patent is hereby incorporated by reference.Comprise that described catalyzer of people such as Ebner and this catalyst system that contains the catalyzer of transition metal of the present invention are favourable, because it is oxidation PMIDA, formaldehyde and formic acid effectively, but the catalyzer of the not all PMIDA of can be used for oxidation all requires to exist expensive precious metal.Therefore, this catalyst system can provide more economical method potentially.Typically, this catalyst system comprise at least about 10 weight % according to US patent No.6, the catalyzer described in 417,133 is more typically at least about 20 weight % and the most about 10-50 weight %.

Select in addition or as another kind of, described catalyst system comprises the catalyzer that contains transition metal composition of the present invention at least about 10 weight %, more typically, the most typically comprise the catalyzer that contains transition metal composition of the present invention of about 20-50 weight % at least about 20 weight %.

The concentration of PMIDA reagent is not crucial in incoming flow.The use of the saturated solution of PMIDA reagent in water is preferred, but for easy operation, and this method also is exercisable under the lower or higher PMIDA reagent concentration in incoming flow.If catalyzer is present in the reaction mixture with finely divided form; then preferably use the reactant of such concentration; make whole reactants and N-((phosphonomethyl)) glycine product remain in the solution, catalyzer can reclaim (for example by filtering) utilization more like this.On the other hand, bigger concentration tends to improve the reactor content flux.Perhaps,, then might use the reactant of bigger concentration, make N-((phosphonomethyl)) the glycine product of a part precipitate if catalyzer exists as static phases (reaction medium and oxygen source are by it).

Should be realized that with respect to many common used in industry methods, the present invention allows to use higher temperature and PMIDA reagent concentration to prepare N-((phosphonomethyl)) glycine, and at utmost reduce the formation of by product simultaneously.In using the usual commercial processes of carbonaceous catalyzer only, useful economically is the formation that farthest reduces the NMG by product, and this by product is to be formed by the reaction between N-((phosphonomethyl)) glycine and the formaldehyde by product.In method based on C catalyst, temperature typically maintains between about 60-90 ℃, and the PMIDA reagent concentration typically maintains and is lower than about 9.0 weight % ([the quality ÷ total reaction quality of PMIDA reagent] * 100%) to realize the effective productive rate of cost and farthest to reduce the generation of refuse.Under this temperature, the highest solubility of N-((phosphonomethyl)) glycine typically is lower than 6.5%.Yet for oxide catalyst of the present invention and reaction process, formaldehyde is oxidized effectively, therefore allows temperature of reaction up to 180 ℃ or higher for the slurry of PMIDA reagent solution and PMIDA reagent.The use of higher temperature and reactor concentration allows reactor output to improve, and has reduced the amount (it must be removed before the separation of solid N-((phosphonomethyl)) glycine) of water, and has reduced the cost of production N-((phosphonomethyl)) glycine.Therefore the present invention provides the economic benefit of comparing with many usual commercial processes.

Usually, can use up to the PMIDA reagent concentration (especially under about 20-180 ℃ temperature of reaction) of about 50 weight % ([the quality ÷ total reactant quality of PMIDA reagent] * 100%) at the most.The preferred PMIDA reagent concentration (special under about 60-150 ℃ temperature of reaction) that uses up to about 25 weight %.More preferably use the PMIDA reagent concentration (special under about 100-130 ℃ temperature of reaction) of about 12-18 weight %.Can use the PMIDA reagent concentration that is lower than 12 weight %; but this is not too economical; because produce N-((phosphonomethyl)) the glycine product of low useful load in the cycle at each reactor; must remove more water, and the N-that is produced ((phosphonomethyl)) the glycine product of per unit will consume the more energy.Lower temperature of reaction (that is, being lower than 100 ℃ temperature) is usually tended to not too favourable, because the solubleness of PMIDA reagent and N-((phosphonomethyl)) glycine product all is lower under this temperature.

The oxygen source of PMIDA oxidizing reaction can be any oxygen-containing gas or the liquid that comprises dissolved oxygen.Preferably, this oxygen source is an oxygen-containing gas.Here " oxygen-containing gas " of Shi Yonging is any gaseous mixture that comprises molecular oxygen, it is optional comprise one or more under reaction conditions not with oxygen or not with the thinner of reactant or product reaction.

The example of this type of gas is an air, pure molecular oxygen, or with the molecular oxygen of helium, argon gas, nitrogen or the dilution of other non-oxidized gas.Because economic aspect, oxygen source most preferably is air, oxygen-rich air or pure molecular oxygen.

According to any common method oxygen is incorporated in the reaction medium, the mode of introducing can remain on desired level with the dissolved oxygen concentration in reaction mixture.If the use oxygen-containing gas, it preferably is introduced in the reaction medium with the mode that contacts between the reaction soln according at utmost increasing gas.This contact can be by disperseing gas or realizing by stirring, shake or other method well known by persons skilled in the art via scatterer such as sintered glass material.

Oxygen feed rate preferably makes the PMIDA oxidizing reaction rate not be subjected to the restriction of oxygen supply.Yet if the concentration of dissolved oxygen is too high, catalyst surface tends to oxidized unfriendly, and then causes more lixiviates of the precious metal that exists and reduce formaldehyde activity (and then causing producing more NMG) in catalyzer.Generally, preferred use make can utilize oxygen at least about a kind of oxygen feed rate of 40%.More preferably, this oxygen feed rate should make being utilized at least about 60% of oxygen.Even more preferably, oxygen feed rate should make being utilized at least about 80% of oxygen.Most preferably, this speed should make being utilized at least about 90% of oxygen.Here the per-cent of the oxygen that is utilized of Shi Yonging equals: (total oxygen consumption rate ÷ oxygen feed rate) * 100%.Term " total oxygen consumption rate " refers to following summation: (i) PMIDA reagent carries out the oxygen consumption rate (" Ri ") that oxidizing reaction forms N-((phosphonomethyl)) glycine product and formaldehyde; (ii) formaldehyde carry out oxidizing reaction form the oxygen consumption rate (" Rii ") of formic acid and (iii) formic acid carry out the oxygen consumption rate (" Riii ") that oxidizing reaction forms carbonic acid gas and water.

In various embodiments of the present invention, oxygen is added in the above-mentioned reactor till most PMIDA reagent is oxidized, uses the oxygen feed rate that reduces then.Consume PMIDA reagent about 75% after, preferably use the feeding rate of this reduction.More preferably, after being consumed, uses by about 80% of PMIDA reagent the feeding rate that reduces.When oxygen is supplied with as pure oxygen or oxygen-rich air, by realize the feeding rate that reduces with (non-enrichment) air purge reactor, preferably under that volume feeding rate that is not more than the volume speed when before air purge, adding pure molecular oxygen or oxygen-rich air, purge.The oxygen feed rate that reduces preferably kept about 2-40 minute, and more preferably from about 5-20 minute, most preferably from about 5-15 minute.When oxygen was added under the speed that reduces, temperature preferably remained under the temperature identical with temperature when reacting before the air purge, or remained under the low a kind of temperature of temperature when reacting before the air purge.Similarly, this pressure remains under the pressure identical with pressure when reacting before the air purge, or remains under the low a kind of pressure of pressure when reacting before the air purge.When finishing, use the oxygen feed rate of reduction to make the removing residue formaldehyde amount that in reaction soln, exists reduce, but can not produce the AMPA of harmful amount owing to oxidation N-((phosphonomethyl)) glycine product near the PMIDA reaction.

Catalyzer comprises in the embodiment of precious metal therein, if sacrifice property reductive agent is kept or is incorporated in the reaction soln, then can observe the loss minimizing of precious metal for the present invention.Appropriate reductant comprises formaldehyde, formic acid and acetaldehyde.Most preferably use formic acid, formaldehyde or their mixture.The experiment of carrying out according to the present invention shows, if a spot of formic acid, formaldehyde or its mixture are added in the reaction soln, then catalyzer will preferentially carry out the oxidation of formic acid or formaldehyde before the oxidation of carrying out PMIDA reagent, and have more activity subsequently when the PMIDA oxidising process is carried out the oxidation of formic acid and formaldehyde.The preferred sacrifice reductive agent that adds about 0.01-5.0 weight % ([the quality ÷ total reactant quality of formic acid, formaldehyde or their mixture] * 100%), more preferably add the sacrifice reductive agent of about 0.01-3.0 weight %, most preferably add the sacrifice reductive agent of about 0.01-1.0 weight %.

In certain embodiments, unreacted formaldehyde and formic acid recirculation are got back in the reaction mixture and are used for subsequent cycle.In this case, the water-based recycle stream that comprises formaldehyde and/or formic acid also can be used to dissolve PMIDA reagent in subsequent cycle.This recycle stream can evaporate from oxidation mixtures so that concentrate and/or crystallization goes out product N-((phosphonomethyl)) glycine and regenerates by water, formaldehyde and formic acid.The top condensation product that contains formaldehyde and formic acid is suitable for recirculation.

As mentioned above, the oxide catalyst of the present invention that is included in the transition metal composition that contains transition metal, nitrogen and carbon that forms on the carbon support of Miao Shuing here, preferably be substantially free of the noble metal active phase, for being effective with oxidation of formaldehyde formic acid, carbonic acid gas and water.Especially, oxide catalyst of the present invention is effective for the oxidation of the by product formaldehyde that produces in the oxidation of N-((phosphonomethyl)) iminodiethanoic acid.More particularly, this type of catalyzer is characterised in that the validity of their catalysis oxidation of formaldehyde, make when containing the representative aqueous solution of having an appointment 0.8 weight % formaldehyde and having a pH of about 1.5 and oxygenant when under about 100 ℃ temperature, contacting in the presence of this catalyzer, at least about 5%, preferably at least about 10%, more preferably at least about 15% even more preferably at least about 20% or even be converted to formic acid, carbonic acid gas and/or water at least about this formaldehyde of 30 weight %.

The oxide catalyst of the present invention that is included in the transition metal composition that contains transition metal, nitrogen and carbon that forms on the carbon support of Miao Shuing here; preferably being substantially free of the noble metal active phase, is effective especially for catalysis formalin phase oxidation formic acid, carbonic acid gas and/or water in the presence of PMIDA reagent such as N-((phosphonomethyl)) iminodiethanoic acid.More particularly; this type of catalyzer is characterised in that the validity of their catalysis oxidation of formaldehyde; make when N-((phosphonomethyl)) iminodiethanoic acid that contains have an appointment 0.8 weight % formaldehyde and about 6 weight % and the representative aqueous solution with pH of about 1.5 and oxygenant when under about 100 ℃ temperature, contacting in the presence of the catalyzer, at least about 50%, preferably at least about 60%, more preferably at least about 70%, more preferably at least about 80% with especially be converted to formic acid, carbonic acid gas and/or water at least about this formaldehyde of 90 weight %.

Typically, the concentration of N-((phosphonomethyl)) glycine in this product mixtures can be up to 40 weight % or higher.Preferably, the concentration of N-((phosphonomethyl)) glycine is about 5-40%, 8-30% more preferably from about, 9-15% more preferably from about again.The concentration of formaldehyde in product mixtures typically is lower than about 0.5 weight %, more preferably less than about 0.3%, again more preferably less than about 0.15%.

After oxidation, catalyzer preferably passes through filtering separation subsequently.N-((phosphonomethyl)) glycine product can for example separate with cooling by a part of evaporation of water by precipitation.

In certain embodiments (for example wherein catalyzer comprises those of precious metal), should be realized that catalyzer of the present invention can be through utilizing after several cycles again, this depends on its oxidized in use degree in surface.Even after catalyzer was by heavy oxidation, it still can utilize by reactivate again.For the reactivation of catalyst on the surface that will have heavy oxidation, preferably at first wash so that remove organism from the surface on the surface.It is preferably to reduce with the above-mentioned mode that the such mode of reducing catalyst is identical after noble metal loading is to the carrier surface.

Generally can be used for any primary alconol is changed into carboxylate salt with the method that further comprises copper-containing active catalyzer introducing of the present invention mutually with being included in the transition metal composition that forms on the carbon support.Here " primary alconol " of Shi Yonging is to comprise any alcohol that is connected in the hydroxyl on the carbon (it is bonded in two hydrogen atoms), i.e. R-CH ₂OH.These class methods obtain carboxylate salt and hydrogen simultaneously with the primary alconol dehydrogenation.Typically, this reaction is to carry out in the reacting by heating district of the alkaline medium that contains primary alconol, alkali and catalyzer prepared in accordance with the present invention is housed.The example of this reaction is that monoethanolamine dehydrogenation in containing the reacting by heating district of KOH forms hydrogen and glycine sylvite:

Another example of this reaction is that diethanolamine (being called " DEA " sometimes in the prior art) dehydrogenation in containing the reacting by heating district of NaOH forms hydrogen and Iminodiacetic acid sodium salt (being sometimes referred to as " DSIDA " in the prior art):

Additional examples is the salt that N-alkyl-monoethanolamine dehydrogenation forms N-alkyl-glycine.This alkyl can be methyl (CH for example ₃).In this case, dehydrogenation product is the salt (that is the salt of sarkosine) of N-methyl-glycine:

Another example is the salt that the trolamine dehydrogenation forms nitrilotriacetic acid(NTA):

Though method of the present invention is effective and useful in the dehydrogenation of any primary alconol basically, method of the present invention is particularly advantageous for the primary alconol that contains amino or contain reactive behavior and other functional group of side reaction takes place easily.Especially, the dehydrogenation of C-N key and follow-up dealkylation take place in beta-alkamine easily, have therefore caused the formation of common undesirable byproduct.In various preferred embodiments of the present invention, primary alconol is alkanolamine (that is, wherein the nitrogen of amine functional group directly is keyed to a kind of compound on the carbon of alkyl alcohol).In this embodiment, this primary alconol preferably has following general formula (I):

Wherein n is the integer of 2-20; R ¹And R ²Be the alkyl of hydrogen, alkyl or replacement independently.

Alkyl can be any group of only being made up of carbon and hydrogen.This alkyl can be a branching or nonbranched, can be saturated or unsaturated, and can comprise one or more rings.Suitable alkyl comprises alkyl, alkenyl, alkynyl and aryl.They also comprise by alkyl, alkenyl, alkynyl and the aryl of other aliphatic series or cyclic hydrocarbon group replacement, as alkaryl, alkene aryl and alkynes aryl.

The alkyl that replaces can be any alkyl, and wherein the carbon atom of this hydrocarbyl group has been replaced or contained the atomic radical replacement of at least one non-hydrogen atom by the atom beyond the dehydrogenation.For example hydrogen atom can be by halogen atom such as chlorine or fluorine atom replacement.Additionally, substituting group that one or more hydrogen atoms can involved Sauerstoffatom or the group that contains Sauerstoffatom substitute, and form for example hydroxyl, ether, ester, acid anhydrides, aldehyde, ketone or carboxylic acid.The group that this hydrogen atom also can be contained nitrogen-atoms substitutes, and forms for example acid amides or nitro.In addition, the substituting group that hydrogen atom can be contained sulphur atom substitutes, and for example forms-SO ₃H.

Typically, R ¹And R ²Be following any independently: hydrogen;-(CH ₂) _x-(CH ₃) _m, x is 0 to about 19 integer (particularly 1-6 and even more particularly 1), m is 1;-(CH ₂) _y-OH, y are 1 integers to about 20 (especially 2-6); (CH ₂) _z-COOH, z are 1 integers to about 19 (especially 1-5); Or (phosphonomethyl).

In certain preferred embodiments, R ¹And R ²All be hydrogen (that is being primary amine) at the amine functional group shown in the general formula (I).This type of pure example is a monoethanolamine.

In other preferred embodiment, R ¹Be hydrogen, R ²It is the alkyl (that is being secondary amine) of alkyl or replacement at the amine functional group shown in the general formula (I).R wherein ²The example that is the primary alconol of alkyl comprises the N-Mono Methyl Ethanol Amine, N-ehtylethanolamine, N-isopropyl alcohol amine, N-butylethanolamine and N-nonyl thanomin.R wherein ²The example that is the primary alconol of the alkyl that replaces comprises wherein R ²Be-(CH ₂) _y-OH and y are 1 primary alconols to the integer of about 20 (more preferably 1-6).This type of pure example is a diethanolamine.R wherein ²Other example that is the primary alconol of substituted hydrocarbon radical comprises N-(2-amino-ethyl) thanomin, N-(3-aminopropyl) thanomin, N-(carboxymethyl) thanomin and N-((phosphonomethyl)) thanomin.The thanomin that N-replaces for example can prepare by using the whole bag of tricks well known in the prior art.For example ketone can with monoethanolamine at H ₂, solvent and noble metal catalyst existence under carry out condensation.This reaction is described in for example Cope, A.C. and Hancock, and E.M.J.Am.Chem.Soc., 64, among the 1503-6 (1942).The thanomin that N-replaces also can prepare by the mono-substituted thanomin of formation that mono-substituted amine (as methylamine) and oxyethane are combined.This reaction is described among the Japanese patent application No.95-141575 by for example Y.Yoshida.

In other preferred embodiment, R ¹And R ²Be the alkyl (that is being tertiary amine) of alkyl or replacement independently at the amine functional group shown in the general formula (I).R wherein ¹And R ²The example that is the primary alconol of alkyl independently comprises N, N-dimethylethanolamine, N, N-diethylethanolamine and N, N-dibutyl thanomin.R wherein ¹Be alkyl and R ²The example that is the primary alconol of substituted hydrocarbon radical comprises wherein R ²Be-(CH ₂) _y-OH and y are 1 primary alconols to the integer of about 20 (more preferably 1-6).This type of alcohol comprises for example N methyldiethanol amine, N-ethyldiethanolamine, N-sec.-propyl diethanolamine and N butyl diethanol amine.R wherein ¹Be alkyl and R ²Other example that is the primary alconol of substituted hydrocarbon radical comprises the N-ethyl, N-(2-amino-ethyl) thanomin; The N-ethyl, N-(2-amino-ethyl) thanomin; With the N-methyl, N-(3-aminopropyl) thanomin.R wherein ¹And R ²The example that is the primary alconol of substituted hydrocarbon radical independently comprises wherein R ¹And R ²Be independently-(CH ₂) _y-OH and y are 1 primary alconols to the integer of about 20 (more preferably 1-6).This type of pure example is a trolamine.R wherein ¹And R ²Other example that is the primary alconol of substituted hydrocarbon radical independently comprises four (2-hydroxyethyl) quadrols and N-((phosphonomethyl))-N-(carboxymethyl) thanomin.

In particularly preferred embodiments, this primary alconol comprises diethanolamine, and dehydrogenation reaction is carried out to form Iminodiacetic acid sodium salt and hydrogen according to the above method.An important factor in this embodiment be unfavorable by product such as sarkosine (promptly; N-methyl-glycine) formation; it tends to influence the downstream process (for example wherein Iminodiacetic acid sodium salt changes into N-((phosphonomethyl)) iminodiethanoic acid, changes into the process of N-((phosphonomethyl)) glycine then) that adopts dehydrogenation product.Have been found that catalyzer of the present invention is dehydrogenated to the sarkosine that use in the process of Iminodiacetic acid sodium salt does not produce significant quantity at diethanolamine, this is owing to there is not nickel in catalyzer.For example typically, use the product of the diethanolamine dehydrogenation that catalyzer of the present invention carries out to contain the by product that comprises sarkosine, glycine and oxalic acid that is no more than about 10 weight %.As additional benefits, catalyzer of the present invention does not need to exist expensive precious metal.

This dehydrogenation reaction is to contact to carry out in the reacting by heating (that is dehydrogenation) that the alkaline medium that contains catalyzer is being housed by primary alconol and catalyzer in the alkaline environment (that is alkaline environment) is distinguished.More specifically, this reaction typically have at least about 11, more preferably at least about 12 with even more preferably carry out in the presence of the highly basic at least about 13 pKa value.Suitable alkali for example comprises alkali metal hydroxide (LiOH, NaOH, KOH, RbOH or CsOH), alkaline earth metal hydroxides (Mg (OH) for example ₂Or Ca (OH) ₂), NaH and tetramethyl ammonium hydroxide.In the middle of these alkali, alkali metal hydroxide (particularly NaOH and KOH and even NaOH more especially) usually is preferred, and this is owing to they solubleness in water under reaction conditions, and their being purchased property easily and the property disposed easily.

The preferred amounts that is incorporated into the alkali in the reaction zone depends on the mole number that for example is incorporated into the primary alconol in the reaction zone.Preferably, by every mole primary hydroxyl group introducing alkali at least about a molar equivalent.Therefore, for example, be monoethanolamine, then preferably by every mole monoethanolamine introducing NaOH at least about 1 mole if alkali is NaOH and primary alconol.If on the other hand, this primary alconol is a diethanolamine, then by the NaOH of at least 2 moles of the preferred introducings of every mole diethanolamine.In particularly preferred embodiments, introduce the alkali of about 1.05-2.0 molar equivalent by each alcoholic extract hydroxyl group.Oxyhydroxide can be for example consider to be worth doing, the form of powder, pellet or the aqueous solution.

This reaction is normally carried out in the liquid medium that comprises the pure and mild solvent that is generally used for alcohol and/or alkali.Alcohol, alkali and catalyzer are introduced in the liquid medium, and this reaction is to carry out in the liquid medium in reaction zone.Basic metal or alkaline earth metal hydroxides can be in every way, and for example the form with bits, powder, pellet or the aqueous solution is introduced in the reaction medium.

Preferably, solvent is to be present in the liquid reaction medium with the ratio that is enough to dissolving whole basically (more preferably, whole) alkali.Solvent also preferably exists with the ratio that is enough to make primary alconol substrate and carboxylate salt product remain solubilized form.

The normally preferred solvent of water, this is owing to its low cost, property obtained and the property disposed easily widely.Alcohol, alkali and solvent preferably carry out blending with such relative proportion, this ratio makes in the beginning in rhythmic reaction cycle or at the upstream extremity of flow reactor, reaction medium contains the reaction medium of alcohol at least about 1 mole/every liter, the reaction medium of the alcohol of typically about 1.8-2.5 mole/every liter, with reaction medium at least about 3 moles alkali/every liter, the alkali of the alcohol of typically about 4-5 mole/every liter.The molar ratio of solvent and alkali and solvent and alcohol typically is respectively between about 0.7 and about 1.2 and between about 0.8 and about 2.0, more typically respectively between about 0.85 and about 1 and between about 1 and about 1.8.In successive back-mixing formula reactive system, solvent, alkali and alcohol preferably are introduced in the reaction medium with the relative proportion that equals above concentration and ratio.

Easily, this catalyzer is to make slurry in liquid reaction medium.Perhaps, contain alkali and alcohol reaction medium flow through the fixed bed of catalyst matrix.In the slurry catalyst system, preferred catalyst loading (that is the preferred concentration of catalyzer in liquid reaction medium) depends on that initial concentration or solvent, catalyzer and the alkali therein of primary alconol substrate for example is introduced in relative rate in the reaction zone.Typically, intermittently or the catalyst loading in the continuous flow reactive system be with respect to the initial primary alconol substrate content of reaction medium at least about 1 weight % (that is [quality of the quality ÷ primary alconol substrate of catalyzer] * 100%).More preferably, this catalyst loading is about 1-70% (more more preferably from about 10-40%) of primary alconol substrate weight.Close in the reactive system in continuous back-mixing, catalyzer and primary alconol preferably are introduced in the reactor according to same or analogous relative proportion.

Preferred catalyst loading depends on that also catalyzer for example is made into the total mass of the alkali lye body medium of slurry.Typically, this catalyst loading be alkaline medium total mass at least about 0.1 weight % (that is, [total mass of the quality ÷ alkaline medium of catalyzer] * 100%), more typically be the alkaline liquid medium total mass at least about 5 weight %.More preferably, this catalyst loading is about 0.1-10 weight % (even 3.5-10 weight % more preferably from about, still even more preferably from about 3.5-5 weight %) of the total mass of alkaline liquid medium.Concentration greater than about 10 weight % is difficult to filter.On the other hand, the concentration that is lower than about 0.1 weight % tends to cause being lower than optimum response speed.

In a preferred embodiment of the invention, pellet type catalyst can join in the aqueous alkaline medium and contact the products of dehydrogenation reactions slurry that comprises catalyzer and Iminodiacetic acid sodium salt to produce with catalyzer by diethanolamine to form slurry.Typically, in this embodiment, this slurry comprises the catalyzer at least about 3.5 weight %, more typically about 3.5-10 weight %.Iminodiacetic acid sodium salt reclaims from the reaction product slurry then.

Tube reaction no matter according to intermittently or continuous mode carry out, preferably drive reaction and finish basically, that is, reach at least about 90%, more preferably at least about 95%, more preferably at least about 98% transformation efficiency.Yet, to select as another kind, reactive system can operated than under the low-conversion, and wherein unreacted alcohol is separated by for example distilling from reaction mixture, and is recycled in the reactor as the part of charging.When reactor is significantly to be lower than under the Quantitative yield rate of alcohol when operating, preferably seek the transformation efficiency of higher alkali, this is because not too separate easily and this alkali of recirculation, especially mineral alkali such as NaOH or KOH.Under this type of situation, alkali can be markedly inferior to 1.0 with the ratio that is introduced in the alcohol in the reactor.If for example transformation efficiency is only 60%, then the ratio of alkali and alcohol can be 0.55-0.65 only.

Reaction is typically at least about 70 ℃, preferably about 120-220 ℃, more preferably from about 140-200 ℃ even more preferably from about 145-155 ℃, still even more preferably carries out under the temperature of about 150 ℃ (especially when primary alconol be that diethanolamine and required product are when being the salt of iminodiethanoic acid).Though can use the temperature of reaction outside these scopes, its result typically is lower than optimum value.For example be lower than under about 120 ℃ temperature, speed of reaction is tended to slow down slowly.And under greater than about 220 ℃ temperature, this catalyzer begins to lose selectivity usually.For example, along with temperature of reaction surpasses about 150 ℃ (particularly along with temperature above about 220 ℃), the dehydrogenation reaction of diethanolamine will tend to form more glycinate by product, therefore for forming required Iminodiacetate product lower selectivity be arranged.

Reaction is preferably carried out under pressure.More particularly, reaction is being enough to prevent that mixture from carrying out under ebullient pressure under the temperature of reaction usually.Under about 120-220 ℃ temperature, pressure is preferably at least about 5kg/cm ², 5-30kg/cm more preferably from about ², 5-20kg/cm more preferably from about ², 8-11kg/cm more preferably from about again ²(that is, about 115-155 pound/square inch), most preferably from about 9.4kg/cm ²(that is, 135 pounds/square inch).Though can use bigger pressure, they are not too favourable usually, because be higher than about 30kg/cm ²Pressure tend to reduce speed of reaction.In certain embodiments, this dehydrogenation reaction zone is to be in to be not more than about 9.5kg/cm ²Under the total pressure of (135 pounds/square inch), wherein the hydrogen dividing potential drop is the about 0kg/cm from when beginning reaction ²(0 pound/square inch) is to the about 9.5kg/cm when reacting peak value ²(135 pounds/square inch) (that is total pressure).

This dehydrogenation reaction preferably carries out (preferably, containing rare gas and/or N in non-oxidizing atmosphere ₂Atmosphere and more preferably N when on being reflected at technical scale, carrying out ₂), (this atmosphere also contains the H that distributes in certain embodiments with the oxidation of avoiding catalyst surface ₂).This preferably owing to the following fact: near the tendency to oxidize of the copper of catalyst surface in reducing activity of such catalysts and selectivity.

Dehydrogenation reaction can be carried out in various intermittences, semi-batch and flow reactor system.The configuration of reactor is not crucial.Suitable common response device configuration comprises for example stirred-tank reactor, fixed-bed reactor, trickle-bed reactor, fluidized-bed reactor, burble reactor, plug flow reactor and parallel flow reactor.Usually, preferred reactor configuration is a stirred-tank reactor.Yet, being imported into situation in the fuel cell for the hydrogen that in dehydrogenation reaction, produces, preferred reactor configuration comprises fixed-bed reactor, then is gas-liquid adsorption.

In rhythmic reaction in the cycle, for each reaction time, typically the alkaline medium at least about diethanolamine/every kg of 200g is introduced in the dehydrogenation reaction zone.Preferably, for each reaction time, be introduced in the dehydrogenation reaction zone at least about the alkaline medium of diethanolamine/every kg of 225g.What typically, be present in diethanolamine in the dehydrogenation reaction zone changes into Iminodiacetic acid sodium salt at least about 5%.

Generally, primary alconol will be converted to the salt of carboxylic acid under the high-conversion rate at least about the salt of being produced/every mole of copper of 2 moles.Preferably, diethanolamine changes into Iminodiacetic acid sodium salt in dehydrogenation reaction zone under the high-conversion rate at least about diethanolamine/every mole of copper of 1 mole.

Reaction mixture preferably filters in the slurry reaction system, isolates catalyzer from liquid medium.Preferred separated catalyst recycle is used for alcohol in the reactor and further changes into carboxylic acid.In making the catalyst reaction system of slurry, the turnover ratio of taking turns by each cycle or each of reactor generally is the diethanolamine/every mole of copper at least about 1 mole.Typically, the phase weekly by reactor or every turnover ratio of taking turns are the diethanolamine/every mole of copper at least about 10 moles, more typically at least about diethanolamine/every mole of copper of 15 moles, more typically are diethanolamine/every mole of copper of about 15-20 mole again.Above-described preferred turnover ratio is that a plurality of rounds of utilizing the repeatedly recirculation of catalyst feed or utilizing catalyzer to pass through reactor realize.In fixed bed or fluidized bed reaction system, high-conversion rate has reflected that catalyst feed or catalyst matrix are discharged and/or for further use the frequency of regenerating from reactive system, and flows through catalyst regeneration or the reactant of the bed between the discharging operation and the volume of product in succession.

Diethanolamine can be continuously or is incorporated into intermittently in the dehydrogenation reaction zone, contacts with catalyzer and forms the product mixtures that comprises Iminodiacetic acid sodium salt.Similarly, product mixtures can take out from product mixtures continuously or intermittently.

When this catalyzer comes recycling by a plurality of reaction times or round and/or re-uses, the migration that is deposited on the metal on the carbon support will be tended to take place in one or more initial reaction cycle or round.In continuous fixed bed or fluidised bed system, this type of migratory aptitude is in taking place in the operating time in early days.Generally, sedimentary metallic particles tends to move to from the part of the less stable on carbon support surface its more stable part.Because the caused this migration of unstable in one or more sites generally is to finish after the early stage round of initial (promptly first and second) reaction time of batch system or continuous system or other operation, so provides a kind of and demonstrated, taken turns the catalyzer of the appropriate stability in inferior in a plurality of reaction times.

When dehydrogenation is when carrying out in the flow reactor system, the residence time in reaction zone can change in wide region, and this depends on employed concrete catalyzer and condition.Similarly, when dehydrogenation is when carrying out in batch reactor, the reaction times typically changes in wide region according to these factors.Usually, this dehydrogenation is equivalent to first order reaction, and the terminal point towards reaction carries out especially.Therefore, the preferred residence time in continuous reaction zone (or the preferred reaction times in the rhythmic reaction district) also will be depended on required transformation efficiency.

Use the various iminodiacetic acid compounds that dehydrogenation catalyst of the present invention produces (an alkali metal salt of preferred iminodiethanoic acid and even more preferably the sodium salt of iminodiethanoic acid) can be as the raw material of acceptable salt on the agricultural of preparation N-((phosphonomethyl)) glycine and N-((phosphonomethyl)) glycine.The salt of iminodiethanoic acid for example can contain HCl, phosphorous acid (H ₃PO ₃) and formaldehyde (CH ₂O) by ization, form N-((phosphonomethyl)) iminodiethanoic acid in the reaction zone, for example US patent No.4 is disclosed such among 775,498 (Gentilcore).N-((phosphonomethyl)) iminodiethanoic acid can and then contact in the presence of oxide catalyst disclosed herein with oxygen, with the carboxymethyl oxicracking, forms N-((phosphonomethyl)) glycine.In addition; N-prepared in accordance with the present invention ((phosphonomethyl)) glycine can further further be handled according to many well-known methods in the prior art, is generally used for acceptable salt on the agrochemistry of N-((phosphonomethyl)) glycine in the weeding glyphosate composition with production.Here " the acceptable salt on the agrochemistry " of Shi Yonging is defined as containing cationic salt, and it allows N-((phosphonomethyl)) glycine negatively charged ion to have agriculturally and useful economically weeding activity.This cationoid can be an alkali metal cation (for example sodium or potassium ion) for example, ammonium ion, sec.-propyl ammonium ion, tetraalkyl ammonium ion, trialkyl sulfonium cation, protonated primary amine, protonated secondary amine, or protonated tertiary amine.

The present invention illustrates by the following example, and these embodiment only are illustrative purposes for example, do not limit the scope of the invention or embodiments of the present invention.

Embodiment

Embodiment 1

Electroless copper on base metal carbide and nitride

This embodiment describes the electroless copper on base metal carbide and nitride in detail.

(Aldrich Chemical Co., Milwaukee WI) are added in the 2L flask that deionized water (200mL) and magnetic stirring bar are housed to form slurry body molybdenum carbide (20.0g).

By Seignette salt (NaKC with reagent grade ₄H ₄O ₆.4H ₂O) (29.99g) (Aldrich Chemical Co., Milwaukee, WI), copper sulfate (CuSO ₄.5H ₂O) (11.79g) (Aldrich Chemical Co., Milwaukee, WI), sodium hydroxide (NaOH) (13.60g) (Aldrich Chemical Co., Milwaukee, 50 weight % solution WI) and 37 weight % formaldehyde (CH ₂O) (11.35mL) (WI) the about 1 liter plating bath of the middle formation of deionized water (950mL) that adds in 2 liters of flasks prepares copper plating solution for Aldrich Chemical Co., Milwaukee.

Plating bath little by little added in the carbide slurry through about 40 minutes time, and the plating bath with about 60mL added in the slurry in wherein per 2.5 minutes.It is by the mobile N on the reaction soln that plating bath adds this plating reaction that neutralizes of carbide slurry to ₂Carry out in the formed nitrogen atmosphere.

The pH of plating bath monitors by using pH meter, to detect the decline by the pH of the caused plating slurry of the consumption of sodium hydroxide.Plating proceeds to slurry pH and reaches till about 8.0.After plating was finished, slurry filtered under nitrogen atmosphere, resulting wet cake in the vacuum of nitrogen purging dry about 8 hours.

Weighing wet cake then is to measure the plating of copper on the body molybdenum carbide.The weight increase of body molybdenum carbide shows that the copper facing rate is the 90%-about 100% of the copper that exists in plating bath.

Embodiment 2 is used to prepare carbon-supported molybdenum carbide (Mo ₂C/C) and carbon-supported molybdenum nitride (Mo ₂N/C) synthesizing of precursor

This embodiment describes the preparation method of the precursor that is used to prepare carbon-supported molybdenum carbide and nitride in detail.

To have 1067m ²The carbon support (20.0g) (Degussa Corporation) of the BET surface-area of/g adds in the 1L beaker that contains deionized water (300mL) and magnetic stirring bar to form slurry.

(Vernon Hills IL) makes by Cole-Parmer Instrument Company in use

Volume pump (

), will in deionized water, contain ammonium molybdate ((NH ₄) ₂MoO ₄) (4.236g) (solution WI) (60ml) adds in the carbon slurry for Aldrich Chemical Co., Milwaukee.Slurry is stirred by mechanical stirrer, and meanwhile this molybdenum solution was added in the carbon slurry with 2.0ml/ minute the speed time through about 30-40 minute.In molybdenum solution added process in the carbon slurry to, (common interpolation WI) was maintained at about 4.0 with the pH of gained mixture for Aldrich Chemical Co., Milwaukee by rare nitric acid (about 5-10mL).In deposition process, stir the carbon slurry and when the pH of slurry is higher than 4.0, add acid with the 5-10ml increment.

After molybdenum solution the process in the carbon slurry of adding to is finished, this slurry stir about 30 minutes.(Aldrich Chemical Co., Milwaukee is about the pH regulator to 3.0 of interpolation with mixture WI), and stir about 30 minutes again by rare nitric acid (2-5mL).

The gained mixture filters and uses the deionized water wash of about 800mL, then wet cake in the vacuum drying oven that nitrogen purging is crossed 120 ℃ of following dry nights.

Embodiment 3 contains the carbon-supported molybdenum carbide (15%Mo of 15 weight % molybdenum carbides ₂Synthesizing C/C)

Present embodiment describes the method for use according to the carbon-supported molybdenum carbide of precursor preparation of the carbon-supported molybdenum carbide of the preparation of program described in the above embodiment 2 in detail.

Carbide precursor (8.0g) is joined in haas troy C (Hastelloy C) tubular reactor of having filled high temperature insulating material, in order to 100cm ³The argon gas that/minute flow velocity is incorporated in the reactor purged about 15 minutes down at about 20 ℃.Thermopair is inserted into the reactor center of using for the precursor material charging.

The temperature of reactor was increased to about 300 ℃ through 30 minutes, and (Airgas Co., St.Louis is MO) with about 100cm with 50%/50% (v/v) mixture of methane and hydrogen in during this period of time ³/ minute speed be incorporated in the reactor.

The temperature of reactor is brought up to about 650 ℃ with about 2 ℃/minute speed then.Reactor is under this temperature and with about 100cm ³/ minute speed is incorporated into 50%/50% (v/v) mixture of methane in the reactor and hydrogen, and (Airgas Co., St.Louis kept about 4 hours in air-flow MO).Homothermic during this period of time in, on carbon support, form the molybdenum carbide composition.

The gained carbide by with about 100cm ³/ minute the speed air-flow that is incorporated into 20%/80% (v/v) mixture of hydrogen in the reactor and argon gas contact and clean.The temperature of reactor kept other approximately 30 minutes down at about 650 ℃, and reactor is at 100cm after this section period ³/ minute argon gas stream under be cooled to about 20 ℃ through time of 90 minutes.

Embodiment 4 contains 15 weight % molybdenum nitride (15%Mo ₂N/C) synthesizing of carbon-supported molybdenum nitride

This embodiment describes the method for use according to the carbon-supported molybdenum nitride of 15% of program described in the above embodiment 2 preparation carbon-supported molybdenum nitride precursor preparation in detail.

Nitride precursor (10.0g) is joined in haas troy C (Hastelloy C) tubular reactor of having filled high temperature insulating material, in order to 100cm ³The argon gas that/minute flow velocity is incorporated in the reactor purged about 15 minutes down at about 20 ℃.

The temperature of reactor was increased to about 300 ℃ through 30 minutes then, and (Airgas Co., St.Louis is MO) with about 100cm with ammonia in during this period of time ³/ minute speed be incorporated in the reactor.

The temperature of reactor is brought up to about 800 ℃ with about 2 ℃/minute speed then.This reactor is under this temperature and at about 100cm ³Kept about 4 hours under the ammonia flow of/minute speed.Homothermic during this period of time in, reactor is with about 100cm ³/ minute speed is incorporated in the air-flow of the ammonia in the reactor and keeps.

On carbon support, form the molybdenum nitride composition.Reactor is at 100cm ³/ minute argon gas in be cooled to about 20 ℃ through time of 90 minutes.

The quality of embodiment 5 plated copper on carbon-supported nitride

The quality of plated copper is to check according to the percentage test of the molybdenum lixiviate from carbon support on according to the carbon-supported metal nitride of the preparation of method described in the above embodiment 4.Prepared carbon-supported nitride contains 10 weight % nitride.More than be to use different top temperature (T under by constant retention time in the nitrogenize described in the embodiment 4 operation at 1 hour _Max) carry out.The result sums up in the following Table 1.

The T that table 1 is changing _MaxResult with Cu plating and Mo lixiviate under 1 hour the retention time

T _max(℃)	700	750	800	850	900
						Cu plating productive rate (%)	＞99	＞99	＞99	＞99	＞99
The weight of Cu increases (%)	66	73	77	85	83
						Mo lixiviate (%)	44	45	23	40	32

Embodiment 6 is copper-plated quality on carbon-supported nitride

The quality of plated copper is to check according to the percentage test of the molybdenum lixiviate from carbon support on according to the carbon-supported metal nitride of the preparation of method described in the above embodiment 4.Prepared carbon-supported metal nitride contains 10 weight % nitride.More than be top temperature (T in the nitrogenize described in the embodiment 4 operation by using 800 ℃ _Max) and 4 hours retention time carry out.The result is summarised in the following table 2.

Table 2 is at 800 ℃ of T _MaxWith the Cu plating under 4 hours retention time and the result of Mo lixiviate

Cu plating productive rate (%)	＞99
		The weight of Cu increases (%)	93
Mo lixiviate (%)	7

Embodiment 7 is copper-plated quality on carbon-supported carbide

The quality of plated copper is to check according to the percentage test of the molybdenum lixiviate from carbon support on according to the carbon-supported metallic carbide of the preparation of method described in the above embodiment 3.Prepared carbon-supported carbide contains 10 weight % carbide.More than be by using different top temperature (T under the constant retention time at 1 hour in the carbonization described in the embodiment 3 operation _Max) carry out.The result is summarised in the following table 3.

The T that table 3 is changing _MaxResult with Cu plating and Mo lixiviate under 1 hour retention time

T _max(℃)	600	650	700	750	800
						Cu plating productive rate (%)	98	＞99	＜5	＜5	0
The weight of Cu increases (%)	47	67	0	0
						Mo lixiviate (%)	58	53

Embodiment 8 is copper-plated quality on carbon-supported carbide

The quality of plated copper is to check according to the percentage test of the molybdenum lixiviate from carbon support on according to the carbon-supported metallic carbide of the preparation of method described in the above embodiment 3.Carbon-supported carbide contains 10 weight % carbide.More than be top temperature (T in the carbonization described in the embodiment 3 operation by 650 ℃ _Max) and 1-8 hour retention time carry out.The result is summarised in the following table 4.

Table 4 is at 650 ℃ T _MaxWith Cu plating and Mo lixiviate result in the retention time that changes

Retention time	1	2	4	8
					Cu plating productive rate (%)	＞99	＞99	＞99
The weight of Cu increases (%)	67	100
					Mo lixiviate (%)	53	1	7

Embodiment 9 is in the stability that is fit to the diethanolamine dehydrogenation is formed carbide carbon-supported under the condition of Iminodiacetic acid sodium salt

Use each the prepared carbon-supported carbide in four kinds of carbon supports to be to use program described below to test according to the above method.

Carrier can be described below:

Carrier	Surface-area (m ²/g)
		No.1	1041
No.2	1150
		No.3	1067
No.4	1567

The dehydrogenation of diethanolamine is to construct and be equipped with back-pressure regulator, H by haas troy C (Hastelloy C) (high strength, nickel based alloy) ₂Carry out in the 300ml autoclave reactor of mass flowmeter and charging stock tank, this charging stock tank allows reagent and rinse water to be added in the reactor in rare gas element.

In order to test the stability of various carbon-supported carbide compositions in dehydrogenation condition, the catalyzer that contains 22 weight %Cu, 3 weight %Pt on carbon support is added in the reactor with carbon-supported carbide composition.

This reactor earlier with argon cleaning (when on technical scale, carrying out this reaction, N ₂Be preferred).Contain sodium hydroxide (99.81g) (Aldrich Chemical Co., Milwaukee, 50 weight % solution WI), the mixture N of diethanolamine (62.50g) (Huntsman Chemicals) and deionized water (75mL) ₂Bubbling purge and and N ₂The deionized water that-bubbling purge is crossed (40mL) is introduced in the reactor together.Reactor is sealed then and use N ₂Flushing.In reaction process, mixture stirs continuously, and this pressure remains on 135 pounds/square inch by using back-pressure regulator, and temperature maintenance is at about 150 ℃.

Reaction was carried out about 3 hours, and took out several samples when the reaction beginning, after reaction is carried out 1.5 hours and after reaction is carried out 3 hours from reactor.

Based on the molybdenum amount of the measured lixiviate from the carbide of the amount of molybdenum in the sample that from reactor, takes out that uses inductively coupled plasma-mass spectrometry to measure, to sample analysis to be determined at the stability of the carbon-supported carbide under the dehydrogenation condition.

Carbon-supported carbide catalyst is explained according to its carrier.For example o.1 catalyst n refers to comprise the carbon-supported carbide catalyst of carrier No.1.Carry out a dehydrogenation cycle with test catalyst No.1, catalyst n o.2 with catalyst n each in o.3, carry out two dehydrogenation cycles simultaneously with test catalyst No.4.First time of the stability of test catalyst No.4 is only to use carbon-supported carbide catalyst to carry out, the 22 weight %Cu, the 3 weight %Pt that are included on the carbon support for second time.

The results are shown in the table 5.The per-cent that in the reaction times is the lixiviate of measuring at 0 o'clock is basically owing to the reaction of unconverted molybdenum oxide and sodium hydroxide.To be included in the reaction times be lixiviate on the lixiviate that existed in 0 o'clock and the possible carbide that forms from reaction process to the per-cent of lixiviate in the reaction times of 90 minutes and 3 hours.For example as following for catalyst n o.1 shown in the table 5, with reaction at first in 90 minutes 2.1% of total weight of molybdenum % corresponding molybdenum lixiviate be lixiviate from the carbide surface that during this time, forms.Although as if the lixiviate in 3 hours reaction times reduces in some cases, based on experimental error, these results show that the lixiviate amount keeps substantially constant after 1.5 hours reaction times.

The stability of table 5 carbon-supported molybdenum carbide under dehydrogenation condition

Catalyzer molybdenum lixiviate (the weight % of total Mo)

	t＝0	T=1.5 hour	T=3 hour
				No.1	1.6％	3.7％	4.5％
No.2	4.4％	6.7％	4.5％
				No.3	3.3％	4.5％	4.4％
No.4 (cycle 1)	4.9％	14.5％
				No.4 (cycle 2)	1.6％	0.9％	0.9％

Table 6 has shown the composition of reactor in sample time.

Table 6

The reactor sample component:

Diethanolamine (DEA)

N-(2-hydroxyethyl) glycine (HEG)

Iminodiethanoic acid (IDA)

Iminodiacetic acid sodium salt (DSIDA)

Embodiment 10 is in the stability that is fit to the diethanolamine dehydrogenation is formed nitride carbon-supported under the condition of Iminodiacetic acid sodium salt

Test according to program described below by using two kinds of prepared carbon-supported nitride of different carbon supports according to the above method.Carrier can be described below:

Carrier	Surface-area (m ²/g)
		No.1	1041
No.2.	1150

In order to test the stability of various carbon-supported combinations of nitrides things in dehydrogenation condition, the catalyzer that contains 22 weight %Cu, 3 weight %Pt on carbon support is added in the reactor with carbon-supported carbide composition.

This reactor earlier with argon cleaning (when on technical scale, carrying out this reaction, N ₂Be preferred).Contain sodium hydroxide (99.81g) (Aldrich Chemical Co., Milwaukee, the mixture N of 50 weight % solution WI), diethanolamine (62.50g) (Huntsman Chemicals) and deionized water (75mL) ₂Bubbling purge and and N ₂The deionized water that-bubbling purge is crossed (40mL) is introduced in the reactor together.Reactor is sealed then and use N ₂Flushing.In reaction process, mixture stirs continuously, and this pressure remains on 135 pounds/square inch by using back-pressure regulator, and temperature maintenance is at about 150 ℃.As H from reaction ₂Produce speed and be reduced to cm ³/ minute the time, with reactor cooling, and with N ₂The deionized water that-bubbling purge is crossed (80mL) adds in the reactor.

Based on the molybdenum amount of the measured lixiviate from the carbide of the amount of molybdenum in the sample that from reactor, takes out, sample is analyzed to be determined at the stability of the carbon-supported nitride under the dehydrogenation condition.

Carbon-supported nitride catalyst is explained according to its carrier.For example o.1 catalyst n refers to comprise the carbon-supported nitride catalyst of carrier No.1.Carry out a dehydrogenation cycle with test catalyst No.1 and No.2.The results are shown in the table 7.

The stability of table 7 carbon-supported molybdenum nitride under dehydrogenation condition

Nitride molybdenum lixiviate (the weight % of total Mo)

	t＝0	t＝1.5	T=3 hour
				No.1	～5％	6.0％	4.4％
No.2	～5％	10.1％	7.5％

In the reaction times is that the lixiviate per-cent measured in 0 o'clock is basically owing to the reaction of unconverted molybdenum oxide and sodium hydroxide.To be included in the reaction times be lixiviate on the lixiviate that existed in 0 o'clock and the possible nitride that forms from reaction process to the per-cent of lixiviate in the reaction times of 90 minutes and 3 hours.For example, as following for catalyst n o.1 shown in, and in about 0.9% of the at first total weight of molybdenum % in 90 minutes of reaction corresponding molybdenum lixiviate be lip-deep lixiviate from the carbide that during this time, forms.Although as if the lixiviate in 3 hours reaction times reduces in some cases, based on experimental error, these results show that the lixiviate amount keeps substantially constant after 1.5 hours reaction times.

Embodiment 11 is copper bearing Preparation of catalysts on carbon-supported molybdenum carbide

Present embodiment describes the Preparation of catalysts that contains carbon-supported molybdenum carbide and copper in detail.

To add to according to the carbon-supported molybdenum carbide (6.70g) with containing 15 weight % molybdenum carbides of the preparation of method described in the above embodiment 3 in the deionized water (200mL) in 1 liter of flask of magnetic stirring bar is housed, form slurry.

By Seignette salt (NaKC with reagent grade ₄H ₄O ₆4H ₂O) (15g) (Aldrich Chemical Co., Milwaukee, WI), copper sulfate (CuSO ₄5H ₂O) (5.90g) (Aldrich Chemical Co., Milwaukee, WI), sodium hydroxide (NaOH) (6.80g) (Aldrich Chemical Co., Milwaukee, 50 weight % solution WI) and 37 weight % formaldehyde (CH ₂O) (5.70mL) (Aldrich Chemical Co., Milwaukee WI) add in the deionized water (450mL) in 1 liter of flask and prepare copper plating solution (the about 500ml of cumulative volume).

Carbide slurry and coating solution are all at nitrogen (N ₂) be cooled to about 2 ℃ in the atmosphere, meanwhile stir with magnetic stirring bar.After cooling, about 30 minutes time of process adds coating solution in the carbide slurry in nitrogen atmosphere gradually, and wherein per minute adds the coating solution of 16mL in the carbide slurry to.After coating solution the process in the carbide slurry of adding to was finished, the gained mixture used magnetic stirring bar about 3 ℃ of following stir abouts 2 hours.Descend by the pH of the caused mixture of consumption of sodium hydroxide and to monitor the plating quality.The pH of mixture is lower than till 8 by using pH meter monitoring and continuation plating to be reduced to up to the pH of mixture.Mixture filters under nitrogen atmosphere, obtains wet cake.Gained wet cake water (200mL) washing, packing, and following dry about 8 hours at 120 ℃ in the vacuum drying oven that purging with nitrogen gas is crossed.

Based on the metal analysis of gained filtrate, record the solid that is obtained and have following composition: 18 weight % copper, 11 weight % carbide, surplus is made of carbon support.(18％Cu-11％Mo ₂C/C)。

Embodiment 12 is copper bearing Preparation of catalysts on carbon-supported molybdenum carbide

To add to according to the carbon-supported molybdenum carbide (6.97g) with containing 15 weight % molybdenum carbides of the preparation of method described in the above embodiment 3 in the deionized water (200mL) in 1 liter of flask of magnetic stirring bar is housed, form slurry.

By Seignette salt (NaKC with reagent grade ₄H ₄O ₆4H ₂O) (15g) (Aldrich Chemical Co., Milwaukee, WI), copper sulfate (CuSO ₄5H ₂O) (5.90g) (Aldrich Chemical Co., Milwaukee, WI) and (6.80g) (Aldrich Chemical Co. of sodium hydroxide (NaOH), Milwaukee, 50 weight % solution WI) add in the deionized water (450mL) in 1 liter of flask and prepare copper plating solution (the about 500ml of cumulative volume).

This carbide slurry and coating solution are all at nitrogen (N ₂) be cooled to 0-2 ℃ in the atmosphere.After cooling, coating solution and carbide slurry mix in nitrogen atmosphere and used the magnetic stirring bar stir about 30 minutes.After stirring, use

Volume pump is with 37 weight % formaldehyde (CH ₂O) (5.70ml) (WI) mixture in the 20ml deionized water added in the slurry that is under about 3 ℃ through about 30 minutes for Aldrich Chemical Co., Milwaukee.

The temperature of mixture is increased to about 13 ℃ through about one hour then, and remain under this temperature mixture become colourless basically till.This cost 10-15 minute, mixture filters under nitrogen atmosphere after this time, obtains wet cake.Wet packing is taken advantage of in gained wet cake water (200mL) washing, and in the vacuum drying oven that purging with nitrogen gas is crossed 120 ℃ dry about 8 hours down.

Based on the metal analysis of gained filtrate, record the solid that is obtained and have following composition: 19 weight % copper, 10 weight % carbide, surplus is made of carbon support.(19％Cu-10％Mo ₂C/C)。

Embodiment 13 is copper bearing Preparation of catalysts on carbon-supported molybdenum carbide

To add to according to the carbon-supported molybdenum carbide (6.30g) with containing 13 weight % molybdenum carbides of the preparation of method described in the above embodiment 3 in the deionized water (200mL) in 1 liter of flask of magnetic stirring bar is housed, form slurry.

By ethylenediamine tetraacetic acid (EDTA) (EDTA, C with reagent grade ₁₀H ₁₆O ₈N ₂) (13.74g) (Aldrich Chemical Co., Milwaukee, WI), copper sulfate (CuSO ₄5H ₂O) (5.90g) (Aldrich Chemical Co., Milwaukee, WI), sodium hydroxide (NaOH) (6.80g) (Aldrich Chemical Co., Milwaukee, 50 weight % solution WI) and 37 weight % formaldehyde (CH ₂O) (0.15mL) add in the deionized water (450mL) in 1 liter of flask and prepare copper plating solution (the about 500ml of cumulative volume).

This carbide slurry and coating solution are all at nitrogen (N ₂) be cooled to 0-2 ℃ in the atmosphere.After cooling, coating solution and carbide slurry mix in nitrogen atmosphere and used the magnetic stirring bar stir about 15 minutes.After stirring, with 37 weight % formaldehyde (CH ₂O) (5.70ml) (WI) mixture in deionized water adds in the mixture for Aldrich Chemical Co., Milwaukee, uses magnetic stirring bar about 2 ℃ of following stir abouts 10 minutes then.

The temperature of mixture then through about 20 minutes time be increased to about 18 ℃ and remain under this temperature mixture become colourless basically till.This cost about 10-15 minute, mixture filters under nitrogen atmosphere after this time, obtains wet cake.Wet packing is taken advantage of in gained wet cake water (200mL) washing, and in the vacuum drying oven that purging with nitrogen gas is crossed 120 ℃ dry about 8 hours down.

Embodiment 14 contains the catalyzer that is deposited on the copper on the carbon-supported molybdenum carbide and is used for diethanolamine is dehydrogenated to Iminodiacetic acid sodium salt

This embodiment describes in detail according to the catalyzer of program described in the above embodiment 11 preparation time through 8 reaction times and is used for Iminodiacetic acid sodium salt is produced in the diethanolamine dehydrogenation

This dehydrogenation is to carry out in the 300ml Parr autoclave continuous stirred tank reactor (CSTR) with intermittence or continuous mode operation.This reactor is to operate with intermittent mode in 8 reaction times of present embodiment each.Back-pressure regulator, H are constructed and be equipped with to this reactor by haas troy C (high strength, nickel based alloy) ₂Mass flowmeter and charging stock tank, the latter allows reagent and rinse water be added in the reactor in atmosphere of inert gases.

Will be according to catalyzer (7.0g), 50 weight % sodium hydroxide (55.90g) (the Aldrich Chemical Co. of the preparation of method described in the above embodiment 7, Milwaukee, WI), diethanolamine (35.11g) (Huntsman Chemicals) and water (42.44g) joins in proper order according to this and form mixture in reactor.

This reactor is set in the maximum volume of about 170ml, and the total amount of the mixture that is added (140.45g) provides suitable hydrogen to break away from.Being in 3000 pounds of/square inch high pressure vessel N2 under the pressure is used for the reaction headspace is become inertia and reaction is adjusted to about 135 pounds/square inch starting pressure.

In reaction process, mixture is stirred continuously and this pressure maintains about 135 pounds/square inch by using the control valve of being made by Badger Research.Temperature of reaction maintains about 150 ℃ in entire reaction course.

Reaction was carried out about 3 hours, in during this period of time in the Brooks flow process thermal mass flow inductor (Model No.5860IA13VB2EA) to be used for the amounts of hydrogen that produces at reaction mixture be basic monitoring reaction.

After reaction is carried out about 3 hours, with reaction mass be cooled to about 90 ℃ and use 0.5 μ m metal sintering frit (Mott Corporation, Hartford, CT) with reactant on the spot with catalyst separating.The sample of reaction mass is analyzed by using high pressure lipuid chromatography (HPLC) (" HPLC ").

Carry out seven additional dehydrogenation cycles according to above condition, wherein the diethanolamine with analog quantity joins in the reactor.

Compare by the actual hydrogen tolerance that will be produced and the hydrogen theoretical amount that produces in reaction mixture that with the amount that joins diethanolamine in the reactor is basic calculation, 1-7 measures level of response by the oxyhydroxide transformation efficiency for reaction time.The results are shown in the following table 8.

The composition from the product sample of

reaction time

1 and 2 that uses that HPLC analyzes is listed in the table 9.

The composition of table 9 dehydrogenation product sample

Cycle No.	1	2
			DEA(mol％)	10.77	11.73
HEG(mol％)	50.59	62.47
			Glycine (mol%)	1.55	1.92
IDA(mol％)	20.09	23.92
			OH transformation efficiency (%)	55	56

The product sample component:

Diethanolamine (DEA)

N-(2-hydroxyethyl) glycine (HEG)

Iminodiethanoic acid (IDA)

The catalyzer that embodiment 15 contains the copper on carbon-supported molybdenum carbide is used for the diethanolamine dehydrogenation is formed Iminodiacetic acid sodium salt

Will be according to catalyzer (7.2g), 50 weight % sodium hydroxide (54.95g) (the Aldrich Chemical Co. of the preparation of method described in the above embodiment 12, Milwaukee, WI), diethanolamine (35.04g) (Huntsman Chemicals) and water (46.74g) joins in proper order according to this and abovely form mixture in the reactor described in the embodiment 14.The dehydrogenation of diethanolamine is undertaken by using with reaction conditions identical in embodiment 14.

6 dehydrogenation cycles are that the diethanolamine that joins in the reactor with similar quantity carries out in each cycle.Based on the oxyhydroxide transformation efficiency that obtains according to method described in the above embodiment 14, be determined at the result of level of response in each of 6 reaction times and be listed in the following table 10.

Table 10

Diethanolamine (DEA)

The catalyzer that embodiment 16 contains the copper on carbon-supported molybdenum carbide is used for the diethanolamine dehydrogenation is formed Iminodiacetic acid sodium salt

Will be according to catalyzer (7.0g), 50 weight % sodium hydroxide (60.52g) (the Aldrich Chemical Co. of the preparation of method described in the above embodiment 13, Milwaukee, WI), diethanolamine (39.16g) (Huntsman Chemicals) and water (49.40g) joins in proper order according to this and abovely form mixture in the reactor described in the embodiment 14.

The dehydrogenation of diethanolamine by use with embodiment 10 in identical reaction conditions carry out.In 3 dehydrogenation cycles, in these cycles, react and carried out respectively about 4,4.5 and 6 hours.Diethanolamine with analog quantity in each cycle joins in the reactor.Based on the oxyhydroxide transformation efficiency that obtains according to method described in the above embodiment 13, be determined at the result of level of response in each of 3 reaction times and be summarised in the following table 11.

Table 11

Embodiment 17 contains the catalyzer that is deposited on the copper on the carbon-supported molybdenum carbide and is used for diethanolamine is dehydrogenated to Iminodiacetic acid sodium salt

This embodiment describes the 12%Cu-13%Mo according to the preparation of program described in the above embodiment 14 in detail ₂The C/D1015 catalyzer was used for Iminodiacetic acid sodium salt is produced in the diethanolamine dehydrogenation through the time of 3 reaction times.

This dehydrogenation is to carry out in the 300ml Parr autoclave continuous stirred tank reactor (CSTR) with intermittence or continuous mode operation.This reactor is to operate with intermittent mode in 3 reaction times of present embodiment each.Back-pressure regulator, H are constructed and be equipped with to this reactor by haas troy C (high strength, nickel based alloy) ₂Mass flowmeter and charging stock tank, the latter allows reagent and rinse water be added in the reactor in atmosphere of inert gases.

Will according to the catalyzer (7.5g) of above enforcement 7 described methods preparations (12 weight % copper and 13 weight % molybdenum carbides and surplus have a 1067m ²The carrier of/g surface-area), 50 weight % sodium hydroxide (59.6g) (Aldrich Chemical Co., Milwaukee, WI), diethanolamine (37.45g) (Huntsman Chemicals) and deionized water (36.10g) add in proper order according to this and form mixture in reactor.

This reactor is set in the maximum volume of about 170ml, and the total amount of the mixture that is added (140.64g) provides suitable hydrogen to break away from.The high pressure vessel N2 that is under 3000 pounds/square inch the pressure is used for the reaction headspace is become inertia and reaction is adjusted to about 135 pounds/square inch starting pressure.

In reaction process, mixture is stirred continuously and this pressure maintains about 135 pounds/square inch by using the control valve of being made by Badger Research.Temperature of reaction is maintained at about 150 ℃ in the reaction time of each.

By the actual hydrogen tolerance that will be produced with the diethanolamine amount in the reactor of joining be basic calculation the theoretical hydrogen tolerance that in reaction mixture, produces relatively, measure level of response by the oxyhydroxide transformation efficiency.In the table 12 below the result of level of response is summarised in in 3 reaction times each.

Table 12

Reaction time	1	2	3
				Theoretical H ₂Generation (liter)	32.1 rise	32.1 rise	32.3 rise
Actual H ₂Generation (liter)	19.9 rise		17.1 rise
				Oxyhydroxide transformation efficiency (%)	62％		53％
Molybdenum lixiviate (the weight % of total Mo)	7.1％	1.9％	0.6％

Embodiment 18 molybdenum carbides are used for the oxidation of N-((phosphonomethyl)) iminodiethanoic acid

With N-((phosphonomethyl)) iminodiethanoic acid (PMIDA) (11.48g) 8.2 weight % solution in water (127.8ml) add in the 1L Parr reactor with the molybdenum carbide of carrying capacity 1.3% (1.84g).Before in adding reactor, molybdenum carbide contacts about 1 hour of helium-atmosphere under about 800 ℃ temperature.

Reactor is pressurized to 60 pounds/square inch in nitrogen atmosphere, reaction mixture is heated to 100 ℃.Be reflected under 100cc/ minute the pure oxygen gas flow and carried out about 1 hour.

From reactor, take out the sample of reaction product and the transformation efficiency of assay determination N-((phosphonomethyl)) iminodiethanoic acid.HPLC analysis revealed PMIDA is about 18.2% to the transformation efficiency of N-((phosphonomethyl)) glycine, and formaldehyde is about 33.9% to the transformation efficiency of formic acid.

The preparation of the molybdenum catalyst that embodiment 19 is carbon-supported

This embodiment describes the preparation method of carbon-supported molybdenum catalyst in detail.

Under about 20 ℃ temperature, gac (10.2g) is joined in the water (160ml).The mixture stir about formed the slurry of carbon support in 40 minutes.

With phospho-molybdic acid (H ₃Mo ₁₂O ₄₀P) (0.317g) form solution in water-soluble (30ml), it is added in the carrier slurry.The mixture that contains phospho-molybdic acid stirred 30 minutes then, and solid filters after this section period, with deionized water wash and following dry about 8 hours at 120 ℃ in a vacuum.

The carbon-supported molybdenum compound of exsiccant carries out restoring operation then in the helium-atmosphere that is containing 5% hydrogen under about 800 or 900 ℃ temperature.

Embodiment 20 carbon-supported molybdenum carbide catalysts are used for the oxidation of N-((phosphonomethyl)) iminodiethanoic acid

This embodiment describes the oxidation that is used for N-((phosphonomethyl)) iminodiethanoic acid according to the carbon-supported molybdenum catalyst of the preparation of method described in the above embodiment 19 in detail.

With N-((phosphonomethyl)) iminodiethanoic acid (PMIDA) (5.74g) 4.1 weight % solution in water (133.8g) join in the 1LParr reactor with the carbon-supported molybdenum catalyst of carrying capacity 0.309% (0.432g).Reactor is pressurized to 60 pounds/square inch in nitrogen atmosphere, reaction mixture is heated to about 100 ℃.

In 100cc/ minute pure oxygen gas flow, allow reaction carry out about 80 minutes.Carry out four reaction times, be used for each of last 3 cycles from the catalyzer in previous cycle.

Analyze for the sample of from the reaction mixture of during third and fourth reaction time, producing, obtaining.The transformation efficiency that the HPLC analysis revealed of these samples PMIDA in third and fourth cycle changes into N-((phosphonomethyl)) glycine is respectively about 86.2% and 86.9%.Formaldehyde is respectively about 30.0% and 34.4% to the transformation efficiency of formic acid in third and fourth cycle.

Embodiment 21 carbon-supported molybdenums are used for the oxidation of N-((phosphonomethyl)) iminodiethanoic acid

With N-((phosphonomethyl)) iminodiethanoic acid (PMIDA) (5.74g) 4.11 weight % solution in water (133.8g) join in the 1L Parr reactor with the carbon-supported molybdenum catalyst of carrying capacity 0.155% (0.216g).

Reactor is pressurized to 60 pounds/square inch in nitrogen atmosphere, reaction mixture is heated to about 100 ℃.In 100cc/ minute pure oxygen gas flow, allow reaction carry out about 15 minutes.

From reaction mixture, obtain sample and analyze.HPLC analysis revealed PMIDA changes into N-((phosphonomethyl)) glycine with about 6.8% transformation efficiency, and formaldehyde changes into formic acid with about 17.4% transformation efficiency.

Embodiment 22

This embodiment describes the preparation of carbon-supported iron-containing catalyst precursor in detail.

To have about 1500m ²The particulate state carbon support (10.0g) of/g Langmuir surface-area joins in the 1 liter of flask that contains deionized water (400ml) and forms slurry.The pH of slurry be about 8.0 and temperature be about 20 ℃.

With iron(ic) chloride (FeCl ₃6H ₂O) (0.489g) join in the 100ml beaker that contains deionized water (30ml) and form clear solution.Ferrous solution little by little adds (that is, with about 2ml/ minute speed) through 15 minutes time.(the common interpolation of 0.1 weight % solution WI) is maintained at about 4-4.4 to the pH of carbon slurry for Aldrich Chemical Co., Milwaukee by sodium hydroxide.0.1 weight % sodium hydroxide solution with about 5mL in the interpolation process of ferrous solution adds in the carbon slurry.The pH of slurry uses pH meter (Thermo Orion Model 290) monitoring.

After ferrous solution adds end of processing in the carbon slurry to, slurry uses mechanical stirring rod (50% output rating) (IKA-Werke RW16Basic) to stir 30 minutes, wherein the pH of slurry uses pH meter to monitor, by dripping 0.1 weight % sodium hydroxide or 0.1 weight %HNO ₃Be maintained at about 4.4.

This slurry is heated to 70 ℃ with about 2 ℃/minute speed then under nitrogen protection, its pH maintains 4.4 simultaneously.Reaching after 70 ℃, slurry pH raises at leisure by add 0.1 weight % sodium hydroxide (5ml) according to following pH distribution mode: pH kept 10 minutes at about 5.0 times, bring up to 5.5, kept about 20 minutes for 5.5 times at pH, with stir about 20 minutes, in during this period of time, reach 6.0 constant pH.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1.0 weight % iron of having an appointment.

Embodiment 23

This embodiment describes the method for use according to the carbon-supported iron-containing catalyst of the precursor preparation of the preparation of program described in the above embodiment 22 in detail.

Ferruginous precursor (5.0g) is joined in the haas troy C tubular reactor of having filled high temperature insulating material.Reactor utilizes with about 100cm ³/ minute the argon gas that is incorporated in the reactor of speed purged about 15 minutes down at about 20 ℃.Thermopair is inserted the reactor center of using for the precursor material charging.

The temperature of reactor is increased to about 300 ℃ through about 15 minutes time then, in during this period of time with acetonitrile and argon gas (Airgas, Inc., Radnor, 10%/90% (v/v) mixture PA) is with about 100cm ³/ minute speed be incorporated in the reactor.The temperature of reactor is increased to about 950 ℃ through time of 30 minutes then, allows 10%/90% (v/v) mixture of acetonitrile and argon gas with about 100cm in during this period of time ³/ minute data rate stream cross reactor.Reactor kept about 120 minutes down at about 950 ℃.Reactor is at about 100cm ³/ minute argon gas stream under be cooled to about 20 ℃ through 90 minutes.

The gained catalyzer contains the 1 weight % iron of having an appointment.

Embodiment 24

This embodiment describes in detail and variously contains precious metal and contain the application that non-noble metal catalyzer is used for PMIDA is oxidized to the process of N-((phosphonomethyl)) glycine.

Preparation contains the catalyzer of 0.5 weight % iron according to program described in the above embodiment 23.Its precursor is by using iron(ic) chloride (FeCl according to program described in the above embodiment 22 ₃6H ₂O) solution in deionized water (60ml) (it contacts with the carbon support slurry) prepares (FeCl ₃6H ₂O).

0.5 weight % iron catalyst is used for catalysis PMIDA and is oxidized to glyphosate (curve 6 of Fig. 8).Its performance and following comparing: (1) according to people's such as Ebner US patent No.6,5% platinum of 417,133 preparations, 2 samples of 0.5% iron particulate state C catalyst, sample 1 and 2 (being respectively the

curve

1 and 4 of Fig. 8); (2) according to the US patent No.4 of Chou, the particulate state C catalyst (curve 3 of Fig. 8) of the called after MC-10 of 696,772 preparations; (3) according to the catalyst precursor that contains 1%Fe of the preparation of program described in the above embodiment 22, it replaces acetonitrile to carry out handling (curve 2 of Fig. 8) according to the Preparation of Catalyst program of describing in embodiment 23 with argon gas; (4) has about 1500m ²The particulate state carbon support of the Langmuir surface-area of/g, the program that it has prepared 1 weight % iron catalyst according to being used to described in the above embodiment 23 is handled (curve 5 of Fig. 8) with acetonitrile.

In all cases, the PMIDA oxidation is to carry out in the 200ml glass reactor that total reaction material (200g) is housed, and this total reaction material contains 5.74 weight %PMIDA (11.48g) and 0.11% catalyzer (0.22g).Oxidation is at 100 ℃ of temperature, 60 pounds/square inch pressure, the stirring velocity and the 150cm of 100 rev/mins (rpm) ³/ minute flow of oxygen speed under carry out working time of 50 minutes.

The highest CO in exhaust ₂Per-cent and the accumulative total CO that is produced ₂All be used as the index of the degree of oxidation of PMIDA, formaldehyde and formic acid in reaction process.

Fig. 8 has shown in first reaction time of using six kinds of different catalysts to carry out CO in exhaust ₂Per-cent.

As shown in Figure 8,0.5 weight % iron catalyst demonstrates than the higher activity of MC10 catalyzer and demonstrates the activity suitable with the 5%Pt/0.5%Fe/C catalyzer.Also shown in Fig. 8, the precursor that the carbon support of acetonitrile treatment and argon gas are handled shows very little activity.Table 13 has shown the CO in exhaust in the reaction time of each sample in the middle of using 6 kinds of catalyst samples ₂With the accumulative total CO that is produced ₂

The accumulation CO of table 13 after 50 minute working time ₂Numerical value

Catalyzer	The highest CO in exhaust ₂％	Accumulative total CO ₂(cm ³)
			5%Pt/0.5%Fe/C, sample 1	?41.45	2140
5%Pt/0.5%Fe/C, sample 2	?37.4	2021
			MC-10	?20.02	1255
The 1%Fe/C that argon gas was handled	?6.29	373
			CH ₃The carbon that CN handled	?8.79	533
0.5％FeCN/C	?33.34	1742

Embodiment 25

The characteristic of the iron-containing catalyst of different iron carrying capacity (0.5%, 0.75%, 1% and 2 weight % iron) is to test in PMIDA is oxidized to the reaction of N-((phosphonomethyl)) glycine.

Test with 0.75 weight % iron catalyst and 2 weight % iron catalysts according to 0.5 weight % iron catalyst of embodiment 24 preparations with according to 1 weight % iron catalyst of embodiment 23 preparations.

0.75% is by using the iron(ic) chloride (FeCl of different amounts according to the program of describing among the above embodiment 22 with the precursor of 2% iron catalyst ₃6H ₂O) prepare, depend on required catalyst loading.For the catalyzer that contains 0.75 weight % iron, prepare the solution of iron(ic) chloride (0.366g) in deionized water (60ml), and contact with the carbon support slurry.

For the catalyzer that contains 2.0 weight % iron, prepare the solution of iron(ic) chloride (0.988g) in deionized water (60ml), and contact with the carbon support slurry.

Each of these catalyzer is to test under the PMIDA oxidation reaction condition described in the embodiment 24.

Fig. 9 has shown the period 1 CO of various catalyzer ₂Distribution plan.The curve 1 of Fig. 9 is corresponding to the period 1 of using the 2%Fe catalyzer, the curve 2 of Fig. 9 is corresponding to the period 1 of using the 1%Fe catalyzer, the curve 3 of Fig. 9 corresponding to the curve 4 of the period 1 of using the 0.75%Fe catalyzer and Fig. 9 corresponding to the period 1 of using the 0.5%Fe catalyzer.As shown in, the catalyzer that contains 0.5 weight % iron demonstrates the highest activity.

Table 14 shows use according to 1 weight % iron catalyst of method described in the embodiment 23 preparation with according to people's such as Ebner US6, the HPLC result of the product mixtures of 5% platinum of 417,133 preparations, the reaction that 0.5% iron catalyst is carried out.This table shows N-((phosphonomethyl)) iminodiethanoic acid (PMIDA), N-((phosphonomethyl)) glycine (Gly), formaldehyde (FM), formic acid (FA), iminodiethanoic acid (IDA), aminomethylphosphonic acid and methylamino methyl-phosphorous acid ((M) AMPA), N-methyl-N-((phosphonomethyl)) glycine (NMG) in reaction mixture, imino-is two-and (methylene radical)-two-phosphonic acids (iminobis) and phosphate anion (PO ₄) content.

The HPLC result of table 14 5% platinum, 0.5% iron, 6,417,133 catalyzer and 1%FeCN/C catalyzer after 50 minute working time

	5％Pt/0.5％Fe/C	1％FeCN/C
			PMIDA(％)	0.0108	ND
Gly (％)	3.76	3.63
			FM (ppm)	1427	6115
FA (ppm)	3030	2100
			IDA (％)	0.0421	0.0058
AMPA/MAMPA (ppm)	758	2231
			NMG (ppm)	78	138
Iminobis (ppm)	230	256
			PO ₄ (ppm)	385	107

Embodiment 26

This embodiment describes the preparation method of the carbon-supported cobalt-containing catalyst precursor that contains 1 weight % cobalt in detail.

To have about 1500m ²The particulate state carbon support (10.0g) of the Langmuir surface-area of/g joins in the 1 liter of flask that contains deionized water (400ml) and forms slurry.The pH of slurry be about 8.0 and temperature be about 20 ℃.

With cobalt chloride (CoCl ₂2H ₂O) (0.285g) (Sigma-Aldrich, St.Louis MO) join in the 100ml beaker that contains deionized water (60m) and form clear solution.Through 30 minutes cobalt liquor is joined in the carbon slurry gradually (promptly with about 2ml/ minute speed).In the interpolation process of cobalt liquor, (the common interpolation of 0.1 weight % solution WI) is maintained at about the pH of carbon slurry between 7.5 and about 8.0 for Aldrich Chemical Co., Milwaukee by sodium hydroxide.0.1 weight % sodium hydroxide solution with about 1ml in the interpolation process of cobalt liquor adds in the carbon slurry.The pH of slurry uses pH meter (Thermo Orion, Model 290) monitoring.

After cobalt liquor added end of processing in the carbon slurry to, slurry was by using mechanical stirring rod (the Model IKA-Werke RW16 Basic) stir about operated 30 minutes under 50% output rating; The pH of slurry is by using the pH meter monitoring and passing through 0.1 weight % sodium hydroxide (1ml) or 0.1 weight %HNO ₃Dropping (1ml) is maintained at about 8.0.Slurry is heated to 45 ℃ with about 2 ℃/minute speed then under nitrogen protection, simultaneously by 0.1 weight % sodium hydroxide (1ml) or 0.1 weight %HNO ₃Dropping (1ml) maintains 8.0 with pH.Reaching after 45 ℃, slurry stirred 20 minutes under the pH of 45 ℃ constant temperature and 8.0 by using aforesaid mechanical stirring rod.Slurry is heated to 50 ℃ then, and its pH is adjusted to 8.5 by adding 0.1 weight % sodium hydroxide solution (5ml); This slurry kept about 20 minutes under these conditions.Slurry is heated to 60 ℃ then, and its pH is adjusted to 9.0 by interpolation 0.1 weight % sodium hydroxide solution (5ml) and also kept under these conditions about 10 minutes.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 1.0 weight % cobalts of having an appointment.

Embodiment 27

This embodiment describes the method for preparing carbon-supported cobalt-containing catalyst according to the precursor of the preparation of program described in the above embodiment 26 by using in detail.

To join in the haas troy C tubular reactor of having filled high temperature insulating material according to the cobalt-containing catalyst precursor (5.0g) of the preparation of method described in the above embodiment 26.Reactor utilizes with about 100cm ³/ minute the argon gas that is incorporated in the reactor of speed purged about 15 minutes down at about 20 ℃.Thermopair is inserted into the reactor center of using for the precursor material charging.

The temperature of reactor is increased to about 700 ℃ then, and (Radnor is PA) with about 20cm for Airgas, Inc. with 50%/50% (v/v) mixture of hydrogen and methane in the period at this section ³/ minute speed be incorporated in the reactor, argon gas is with about 100cm ³/ minute speed introduce.This reactor kept about 120 minutes down at about 700 ℃.

Reactor is at about 100cm ³/ minute argon gas stream under be cooled to about 20 ℃ through 90 minutes.

The catalyzer of gained contains the 1 weight % cobalt of having an appointment.

Also,, contain the catalyzer of 1% cobalt from precursor preparation according to the preparation of method described in the embodiment 26 by using acetonitrile according to method described in the embodiment 23.

Embodiment 28

The performance of the cobalt-containing catalyst of various cobalt carrying capacity (0.75%, 1%, 1.5% and 2%) is to test in the oxidizing reaction of the PMIDA under the condition described in the above embodiment 24.According to containing the catalyzer of 1% cobalt by using the acetonitrile preparation in the method described in the embodiment 27.

According to required catalyst loading, by using the cobalt chloride (CoCl of different amounts ₂2H ₂O), the precursor for preparing 0.5%, 0.75% and 2 weight % cobalt catalyst according to program described in the above embodiment 26.Prepare this catalyzer according to the program described in the embodiment 27 by using acetonitrile then.

For the catalyzer that contains 0.75 weight % cobalt, preparation contains the solution of cobalt chloride (0.214g) in deionized water (60ml), and contacts with the carbon support slurry.

For the catalyzer that contains 1.5 weight % cobalts, preparation contains the solution of cobalt chloride (0.428g) in deionized water (60ml), and contacts with the carbon support slurry.

For the catalyzer that contains 2.0 weight % cobalts, preparation contains the solution of cobalt chloride (0.570g), and contacts with the carbon support slurry.

Figure 10 has shown the period 1 CO that uses various catalyzer ₂Distribution plan.The curve 1 of Figure 10 is corresponding to the period 1 of using the 0.75%Co catalyzer, the curve 2 of Figure 10 is corresponding to the period 1 of using the 1%Co catalyzer, the curve 3 of Figure 10 corresponding to the curve 4 of the period 1 of using the 1.50%Co catalyzer and Figure 10 corresponding to the period 1 of using the 2.0%Co catalyzer.

Just as shown in Figure 10, the catalyzer that contains the 1-1.5% cobalt demonstrates the highest activity.

Use four PMIDA reaction times of 1% cobalt catalyst and use according to people such as Ebner at US patent No.6, the HPLC result of the product materials flow of at first four reaction times of the 5%Pt/0.5%Fe/C catalyzer of the preparation of method described in 417,133 sums up in the following Table 15.

This table show N-((phosphonomethyl)) iminodiethanoic acid (GI), N-((phosphonomethyl)) glycine (Gly), formaldehyde (FM), formic acid (FA), iminodiethanoic acid (IDA), aminomethylphosphonic acid and methylamino methyl-phosphorous acid ((M) AMPA), N-methyl-N-((phosphonomethyl)) glycine (NMG), the imino-in the reaction mixture in each cycle two-(methylene radical)-two-phosphonic acids (iminobis) and phosphate anion (PO ₄) content.

The HPLC result of table 15 5%Pt/0.5%Fe/C and 1%CoCN/C catalyzer after 50 minute working time

Embodiment 29

This embodiment has contrasted 1% iron catalyst according to the preparation of method described in the embodiment 23, use 1% cobalt catalyst of acetonitrile preparation according to method described in the embodiment 27, according to people US patent No.6 such as Ebner, 417, the particulate state C catalyst that contains 5 weight %Pt, 0.5 weight % iron of 133 preparations, and according to the US patent No.4 of Chou, the stability of the particulate state C catalyst of the called after MC-10 of 696,772 preparations.

Each catalyzer be used for above embodiment 24 for the PMIDA oxidation under a plurality of reaction times described conditions in.

Figure 11 has shown the CO in exhaust in each of four reaction times of using 1% iron catalyst to carry out (corresponding mark) in addition ₂Per-cent.

Figure 12 has shown the CO in exhaust in each of four reaction times of using 1% cobalt catalyst to carry out (corresponding mark) in addition ₂Per-cent.

Figure 13 has shown the CO in exhaust in each of six reaction times of using the 5%Pt/0.5%Fe/C catalyzer to carry out (corresponding mark) in addition ₂Per-cent.

Figure 14 has shown the CO in exhaust in each of two reaction times of using the MC-10 catalyzer to carry out (corresponding mark) in addition ₂Per-cent.

Ferruginous catalyzer has shown the decline on activity after first cycle, may be owing to the over oxidation of catalyzer.Do not have to observe slight deactivation in the cycle subsequently of over oxidation at catalyzer.5%Pt/0.5%Fe/C is the most stable.1% cobalt catalyst demonstrates with the 5%Pt/0.5%Fe/C catalyzer similarly stable.The MC10 catalyzer demonstrates the poorest stability, even also is like this not having under the over oxidation situation of catalyzer.

Embodiment 30

This embodiment describes various carbon-supported metallic Preparation of catalysts methods in detail.

According to describing embodiment 22 disclosures of iron-containing catalyst precursor preparation method in detail, just on pH and heating schedule, change slightly generally, prepare the precursor of the catalyzer that is used to contain vanadium, tellurium, molybdenum, tungsten, ruthenium and cerium according to the sedimentary metal of want.

The preparation of vanadium precursor: with Na ₃VO ₄10H ₂O (0.721g) adds in the 100ml beaker that contains deionized water (60ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 3.4-3.7 by the common interpolation of 0.1 weight % salpeter solution.Nitric acid with about 5ml in the interpolation process of vanadium solution adds in the carbon slurry.After vanadium solution adds end of processing in the carbon slurry to, this slurry stirred 30 minutes by use the mechanical stirring rod (Model IKA-Werke RW16 Basic) operate under 50% output rating, and the pH of slurry is by using aforesaid pH meter and monitor and being maintained at about 3.6 by nitric acid (0.1 weight % solution) interpolation (2ml).

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % vanadium of having an appointment.

The preparation of tellurium precursor: with Te (OH) ₆(0.092g) add in the 100ml beaker that contains deionized water (60ml) and form solution, the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 6.5-6.9 by the common interpolation of 0.1 weight % solution of sodium hydroxide.0.1 weight % sodium hydroxide solution with about 2ml in the interpolation process of tellurium solution adds in the carbon slurry.After tellurium solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry uses pH meter to monitor and is maintained at about 6.7 by interpolation 0.1 weight % sodium hydroxide solution (1-2ml).

This pH respectively kept 10 minutes at 6.0,5.0,4.0,3.0,2.0 and 1.0 pH.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 1 weight % tellurium of having an appointment.

The preparation of molybdenum precursor: with (NH ₄) ₂MoO ₄(0.207g) add in the 100ml beaker that contains deionized water (50ml) and form solution, the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 1.5-2.0 by the common interpolation of 0.1 weight % salpeter solution.0.1 weight % nitric acid with about 5ml in the interpolation process of molybdenum solution adds in the carbon slurry.After molybdenum solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry is by using the pH meter monitoring and being maintained at about 2.0 by adding 0.1 weight % nitric acid.This pH is increased to 3.0 by adding 0.1 weight % sodium hydroxide then, keeps 20 minutes at 3.0 times, brings up to 4.0 and kept 20 minutes at 4.0 times by adding 0.1 weight % sodium hydroxide solution.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 1 weight % molybdenum of having an appointment.

The preparation of tungsten precursor: with (NH ₄) ₆W ₁₂O ₃₉2H ₂O (0.135g) adds in the 100ml beaker that contains deionized water (60ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 3.0-3.2 by the common interpolation of 0.1 weight % sodium hydroxide solution.Nitric acid with about 2ml in the interpolation process of tungsten solution adds in the carbon slurry.After tungsten solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry is by using the pH meter monitoring and being maintained at about 3.0 by adding 0.1 weight % salpeter solution.

This pH is reduced to 2.5 by adding 0.1 weight % salpeter solution then, keeps 10 minutes at 2.5 times, is reduced to 2.0 and kept 10 minutes at 2.0 times by adding 0.1 weight % salpeter solution.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 1 weight % tungsten of having an appointment.

The preparation of ruthenium precursor: with RuCl ₃2H ₂O (0.243g) adds in the 100ml beaker that contains deionized water (50ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 3.0 to about 3.5 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide with about 1ml in the interpolation process of ruthenium solution adds in the carbon slurry.After ruthenium solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry is by using the pH meter monitoring and being maintained at about 3.5 by adding 0.1 weight % salpeter solution.

This pH is increased to 4.2 by adding 0.1 weight % sodium hydroxide (1ml) then, kept 10 minutes at 4.2 times, be increased to 5.0 by adding 0.1 weight % sodium hydroxide solution (1ml), kept 10 minutes at 5.0 times, be increased to 5.7 and kept 10 minutes by adding 0.1 weight % sodium hydroxide (1ml) at 5.7 times.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % ruthenium of having an appointment.

The preparation of cerium precursor: with Ce (NO ₃) ₃6H ₂O (0.117g) adds in the 100ml beaker that contains deionized water (50ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 7.0-7.5 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide with about 1ml in the interpolation process of cerium solution adds in the carbon slurry.After cerium solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and being maintained at about 7.5 by interpolation 0.1 weight % sodium hydroxide solution (1ml).

This pH is increased to 8.0 by adding 0.1 weight % sodium hydroxide (1ml) then, kept 20 minutes at 8.0 times, be increased to 9.0 by adding 0.1 weight % sodium hydroxide (1ml), kept 20 minutes at 9.0 times, be increased to 10.0 and kept 20 minutes by adding 0.1 weight % sodium hydroxide solution (1ml) at 10.0 times.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % cerium of having an appointment.

According to describing embodiment 26 disclosures of cobalt-containing catalyst precursor preparation method in detail, just on pH and heating schedule, change slightly generally, prepare the precursor that is used to contain nickel, chromium, manganese, magnesium, copper and silver-colored catalyzer according to the sedimentary metal of want.

The preparation of nickel precursor: with NiCl ₂6H ₂O (0.409g) adds in the 100ml beaker that contains deionized water (60ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 7.5 to about 8.0 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide with about 2ml in the interpolation process of nickel solution adds in the carbon slurry.After nickel solution added end of processing in the carbon slurry to, slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and being maintained at about 8.0 by interpolation 0.1 weight % sodium hydroxide solution (1ml).This slurry is heated to 40 ℃ with about 2 ℃/minute speed then under nitrogen protection, by adding 0.1 weight % sodium hydroxide solution its pH is maintained 8.5 simultaneously.Reaching after 60 ℃, this slurry stirred 20 minutes under the pH of 40 ℃ constant temperature and 8.5.Slurry is heated to 50 ℃ of pH with it then and is adjusted to 9.0 by adding sodium hydroxide solution (2ml); Slurry kept about 20 minutes under these conditions.Slurry is heated to 60 ℃ then, and its pH is adjusted to 10.0 and kept under these conditions about 20 minutes by adding sodium hydroxide solution (2ml).

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % nickel of having an appointment.

The preparation of chromium precursor: with CrCl ₃6H ₂O (0.517g) adds in the 100ml beaker that contains deionized water (50ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry maintains about 7.0 to about 7.5 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide with about 1ml in the interpolation process of chromium solution adds in the carbon slurry.After chromium solution added end of processing in the carbon slurry to, this slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and maintaining about 7.5 by adding sodium hydroxide.This slurry is heated to 60 ℃ with about 2 ℃/minute speed then under nitrogen protection, pass through to add its pH of 0.1 weight % sodium hydroxide maintenance of 2ml simultaneously 8.0.

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % chromium of having an appointment.

The preparation of manganese precursor: with MnCl ₂4H ₂O (0.363g) adds in the 100ml beaker that contains deionized water (60ml) and forms solution, and the latter contacts with the carbon support slurry.The common interpolation of 0.1 weight % solution by sodium hydroxide is maintained at about 7.5 to about 8.0 with the pH of carbon support slurry.Sodium hydroxide solution with about 1ml in the interpolation process of manganese solution adds in the carbon slurry.After manganese solution added end of processing in the carbon slurry to, this slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and maintaining about 7.4 by adding sodium hydroxide.This slurry is heated to 45 ℃ with about 2 ℃/minute speed then under nitrogen protection, by adding 0.1 weight % sodium hydroxide solution its pH is remained on 8.0 simultaneously.Reaching after 60 ℃, this slurry stirred 20 minutes under the pH of 50 ℃ constant temperature and 8.5.Slurry is heated to 55 ℃ then, and its pH is adjusted to 9.0 by adding sodium hydroxide solution (2ml); Slurry kept about 20 minutes in these conditions.Slurry is heated to 60 ℃ then, and its pH is adjusted to 9.0 and kept under these conditions about 20 minutes by adding sodium hydroxide solution (1ml).

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % manganese of having an appointment.

The preparation of magnesium precursor: with MgCl ₂6H ₂O (0.420g) adds in the 100ml beaker that contains deionized water (50ml) and forms solution, and the latter contacts with the carbon support slurry.The pH of carbon support slurry is maintained at about 8.5-9.0 by the common interpolation of 0.1 weight % solution of sodium hydroxide.Sodium hydroxide solution with about 5ml in the interpolation process of magnesium solution adds in the carbon slurry.After magnesium solution added end of processing in the carbon slurry to, this slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and maintaining about 8.5 by interpolation 0.1 weight % sodium hydroxide (1ml).

The pH of slurry is increased to 9.0 and kept 30 minutes at 9.0 times by adding 0.1 weight % sodium hydroxide solution (1ml).

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.Precursor contains the 1 weight % magnesium of having an appointment.

The preparation of copper precursors: with CuCl ₂(1.11g) add in the 100ml beaker that contains deionized water (60ml) and form solution, the latter contacts with the carbon support slurry.The pH of carbon support slurry maintains about 6.0 to about 6.5 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide with about 1ml in the interpolation process of copper solutions adds in the carbon slurry.After copper solutions was added end of processing in the carbon slurry to, this slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and maintaining about 6.5 by adding sodium hydroxide.This slurry is heated to 40 ℃ with about 2 ℃/minute speed then under nitrogen protection, by adding 0.1 weight % sodium hydroxide solution its pH is maintained 7.0 simultaneously.Reaching after 40 ℃, slurry stirred 20 minutes under the pH of 40 ℃ constant temperature and 7.0.Slurry is heated to 50 ℃ of pH with it then and is adjusted to 7.5 by adding 0.1 weight % sodium hydroxide solution (1ml); This slurry was kept about 20 minutes under these conditions.The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 5 weight % copper of having an appointment.

The preparation of silver precursor: with AgNO ₃(0.159g) add in the 100ml beaker that contains deionized water (60ml) and form solution, the latter contacts with the carbon support slurry.Common interpolation by 0.1 weight % salpeter solution is maintained at about 4.0 to about 4.5 with the pH of carbon support slurry.Salpeter solution with about 2ml in the interpolation process of silver-colored solution adds in the carbon slurry.After silver-colored solution added end of processing in the carbon slurry to, this slurry stirred 30 minutes, and wherein the pH of slurry is by using pH meter and monitor and maintaining about 4.5 by interpolation salpeter solution (2ml).

The gained mixture filters and uses a large amount of deionized water (about 500ml) washing, wet cake in vacuum drying oven in about 16 hours of 120 ℃ of dryings.This precursor contains the 1 weight % silver of having an appointment.

Each preparation among the catalyst precursor described in the above embodiment 23 contains the metallic catalyzer of 1 weight % metal (is 5 weight % for copper).

Embodiment 31

In the PMIDA oxidation, testing under the condition described in the embodiment 24 according in the catalyzer of method described in the embodiment 30 preparation each.

The highest CO in exhaust ₂Total CO that per-cent is formed and produced in the reaction process at 50 minutes ₂Be used to weigh activity of such catalysts.

The results are shown in the following table 16.

The period 1 reaction result of the various MCN catalyzer of table 16

Catalyzer	CO in exhaust ₂max	Total CO after 50 minutes ₂(cm ³)
			1％FeCN/C	25.93	1624
1％CoCN/C	36.5	1571
			1％NiCN/C	7.36	343
1％VCN/C	11.69	676
			1％CrCN/C	34.88	1809
1％MnCN/C	22.22	1526
			5％CuCN/C	28.45	1571
1％MoCN/C	10.92	753
			1％WCN/C	11.8	684
1％MgCN/C	13.4	830
			1％TeCN/C	10.12	648
1％AgCN/C	12.09	817
			1％RuCN/C	17.77	1041
1％CeCN/C	16.54	1282

Carbon-supported cobalt-containing catalyst and chromium-containing catalyst demonstrate the highest PMIDA oxidation activity.

Embodiment 32

This embodiment describes various carbon-supported catalyzer in detail and is used for the formaldehyde of the PMIDA oxidising process under the condition described in the embodiment 24 and the validity in the formic acid oxidation.

Two kinds of methods are used for estimating the activity of various carbon-supported metallic carbide-nitride catalysts in the oxidation of formaldehyde and formic acid: the HPLC of reaction product analyzes and CO ₂Drop point is measured.The drop point measurement is to observe exhaust CO ₂The moment of the unexpected reduction of forming is by this deflated CO ₂Total amount.As shown in Figure 15, according to people US patent No.6 such as Ebner, 417, the 133 particulate state C catalysts that contain 5%Pt/1%Fe that make are created in 1500-1600cm under the PMIDA of embodiment 24 oxidizing condition ³CO ₂CO about total amount ₂Drop point (curve 1 of Figure 15).Also as shown in Figure 15, use the catalyzer that contains 1% cobalt of acetonitrile preparation to be presented under the PMIDA oxidizing condition of embodiment 24 according to method described in the above embodiment 27 at 1300cm ³About CO ₂Drop point (curve 2 of Figure 15).

According to people US patent No.6 such as Ebner, the 5%Pt/1%Fe catalyzer of 417,133 preparations is at CO ₂Increase 200-300cm on the total amount ³, this can be owing to the more polyoxyization of the formic acid of comparing with 1% cobalt catalyst.

Table 17 has shown the HPLC result by the PMIDA oxidation products of the various catalyzer that use the preparation of method described in the above embodiment 31: 1 weight % cobalt, 1 weight % manganese, 5 weight % copper, 1 weight % magnesium, 1 weight % chromium, 1 weight % molybdenum and 1 weight % tungsten.Carbon-supported cobalt carbide-nitride catalyst shows the highest oxidation of formaldehyde activity.

The HPLC result of table 17 various MCN catalyzer after 50 minute working time

Preparation contain 50 weight % according to method described in the embodiment 27 use 1 weight % cobalt catalyst of acetonitrile preparation and 50 weight % at catalyst mixture according to a kind of catalyzer among 1% nickel, 1% vanadium, 1% magnesium and the 1% tellurium catalyzer of embodiment 31 preparations, and under the PMIDA oxidizing condition described in the embodiment 24, test with the activity of further test for the oxidation of formaldehyde and formic acid.For in 4 kinds of catalyst mixtures each, observe about 1300cm ³Drop point.

Embodiment 33

This embodiment describes various promotor and the PMIDA oxidation of using 1% prepared cobalt catalyst of acetonitrile to combine to be used for according to method described in the above embodiment 27 under condition described in the embodiment 24 in detail.

The promotor of test is: Bismuth trinitrate (Bi (NO ₃) ₃), bismuth oxide (Bi ₂O ₃), tellurium oxide (TeO ₂), iron(ic) chloride (FeCl ₃), nickelous chloride (NiCl ₂), copper sulfate (CuSO ₄), ammonium molybdate ((NH ₄) ₂MoO ₄), and ammonium tungstate ((NH ₄) ₁₀W ₁₂O ₄₁).

Promotor is to be introduced in the reaction mixture when begin reaction time.This promotor is to be introduced in the reaction mixture with the various carrying capacity shown in the table 18.

The highest CO of measurement in exhaust stream ₂Concentration and accumulation CO ₂Numerical value is to measure catalytic activity and record CO ₂Drop point is to measure the activity of catalysis formic acid oxidation.Table 18 has shown the highest CO in exhaust ₂With the CO that in first 50 minute reaction time, produces ₂Total amount.These catalyzer CO separately ₂Drop point is at about 1300cm ³And 1350cm ³Between.

The table 18 period 1 reaction result of the adulterated 1%CoCN/C of promotor (0.021g) catalyzer

Embodiment 34

This embodiment describes preparation method and their uses in the PMIDA oxidation of the carbon-supported carbide-nitride catalyst of bimetal type in detail.

Prepare the catalyzer that contains 1 weight % cobalt and 0.5 weight % iron according to the method described in the above embodiment 27 by using acetonitrile.By according to above respectively in the method described in embodiment 26 and 22, prepare the precursor of 1% cobalt and 0.5% iron catalyst by the sequential aggradation of each metal.

Similarly, prepare the catalyzer that contain 1% cobalt and 0.5% cerium in embodiment 27 described methods by using acetonitrile according to above.By according to above respectively in the method described in embodiment 26 and 30, prepare the precursor of 1% cobalt and 0.5% cerium catalyst by the sequential aggradation of each metal.

According to the above catalyzer that contains 1% cobalt and 0.5% bronze medal in embodiment 27 described method preparations.By according to above respectively in the method described in embodiment 26 and 30, prepare the precursor of 1% cobalt and 0.5% copper catalyst by the sequential aggradation of each metal.

In these catalyzer each is to test in the PMIDA oxidation under the condition of describing in embodiment 24 through four cycles.For in these cycles each, use these catalyzer separately, measure in order to produce 1300cm ³CO ₂The needed time.In order to contrast purpose, 1 weight % cobalt and 1.5 weight % cobalt catalyst make according to method described in the embodiment 28 separately, also test in such a way.The results are shown among Figure 16.As shown in Figure 16,1.5% cobalt catalyst has the activity lower than 1% cobalt catalyst, but demonstrates bigger stability.Compare with each cobalt catalyst, cobalt-cerium catalyst demonstrates improved stability but lower activity is arranged.In a word, the result shows that cobalt, cobalt-iron and cobalt-cerium catalyst have similar oxidation of formaldehyde activity.

The results are shown in Table 19 for the HPLC of the product when using 1.5% cobalt catalyst and 1.5% cobalt/0.5% copper catalyst.Compare with carbon-supported cobalt carbide-nitride catalyst, carbon-supported cobalt-copper catalyst changes into formic acid with more formaldehyde.

The HPLC result of table 19 1.5%CO/C and 1.5%Cu/C catalyzer after 50 minute working time

Embodiment 35

This embodiment describes in detail according to people US patent No.6 such as Ebner; the application of 1: 1 mixture in the oxidation of N-((phosphonomethyl)) iminodiethanoic acid that uses the acetonitrile preparation according to method described in the above embodiment 27 of the 5%Pt/0.5%Fe catalyzer of 417,133 preparations and the carbon-supported catalyzer that contains 1 weight % cobalt.

The preparation mixture (0.210g), it contain 50 weight % according to people US patent No.6 such as Ebner, 417,133 the preparation particulate state C catalyst that contains 5 weight % platinum and 0.5 weight % iron and 1 weight % cobalt catalyst (0.105g).Catalyst mixture is through testing in the PMIDA oxidation under the condition described in the embodiment 24 six reaction times.According to people US patent No.6 such as Ebner, the particulate state C catalysts that contain 5 weight % platinum and 0.5 weight % iron of 417,133 preparations are also through testing in the PMIDA oxidation under the listed condition in embodiment 24 six reaction times.

The highest CO in exhaust ₂The CO that is produced in ratio, among these reaction times each ₂Total amount, the residual formaldehyde content in reaction, the formic acid content in reaction mixture and platinum lixiviate are summed up in the following Table 20.

Table 20

Catalyst mixture is brought into play in the period 1 with the 5%Pt/1%Fe catalyzer and is similarly acted on, but catalyst mixture demonstrates lower accumulation CO ₂Numerical value may be owing to the less oxidation of formic acid.In rest period, the catalyst mixture performance similarly acts on 1 weight % cobalt catalyst, and demonstrates deactivation, also has gathering of formic acid.Metal analysis shows minimum Pt lixiviate, and platinum deactivation is described.

Embodiment 36

This embodiment describes the deposition of platinum on the catalyzer that contains 1 weight % cobalt that uses the acetonitrile preparation according to embodiment 27 described methods in detail.

To join in the 1 liter of flask that contains deionized water (400ml) according to the sample (4.72g) of 1 prepared weight % cobalt catalyst of the above method of in embodiment 27, describing and form slurry.

With H ₂PtCl ₆2H ₂O (0.282) is dissolved in and forms clear solution in the deionized water (80ml).Gradually platinum solution is added in the slurry to (that is, with about 2ml/ minute speed) through 40 minutes times.The pH of slurry is maintained at about 3.8-4.4 by the common interpolation of 0.1 weight % sodium hydroxide solution.0.1 weight % sodium hydroxide solution with about 2ml in the interpolation process of platinum solution adds in the slurry.

After solution added end of processing in the slurry to, this slurry stirred 30 minutes, and the pH of slurry is maintained at about 4.4 by adding 0.1 weight % sodium hydroxide solution.

This slurry is heated to 70 ℃ with about 2 ℃/minute speed then under nitrogen protection, its pH maintains 4.4 simultaneously.Reaching after 70 ℃, the pH of this slurry improves by add 0.1 weight % sodium hydroxide solution according to following distribution mode: pH kept 10 minutes at about 5.0 times after adding the 1ml sodium hydroxide solution, be increased to 5.5 and under this level, kept about 20 minutes by the sodium hydroxide solution that adds 1ml, with stir about 20 minutes, be increased to 6.0 and kept 10 minutes by the 0.1 weight % sodium hydroxide solution that adds 1ml.With NaBH ₄(0.38g) 12 weight % solution in deionized water (10ml) add in the slurry with 2ml/ minute speed.This slurry is heated to 70 ℃ then under nitrogen protection when stirring.

The gained mixture filters and uses the deionized water wash of q.s, and wet cake is following dry about 16 hours at 120 ℃ in vacuum drying oven.

Behind precursor deposition, catalyst made from platonic (5.0g) is joined above in the tubular reactor described in the embodiment 23.Reactor utilizes with about 100cm ³/ minute the argon gas that is incorporated in the reactor of speed purged about 15 minutes down at about 20 ℃.Thermopair is inserted into the reactor center that the adding catalyzer is used.

The temperature of reactor was increased to about 850 ℃ through 120 minutes, in during this period of time with 5%/95% (v/v) mixture of hydrogen and argon gas with about 100cm ³/ minute speed be incorporated in the reactor.

This catalyzer contains have an appointment 2.5 weight % platinum and 1 weight % cobalt.

Embodiment 37

This embodiment describes platinum and the deposition of iron on the catalyzer that contains 1 weight % cobalt that uses the acetonitrile preparation according to embodiment 27 described methods in detail.

The sample of 1 weight % cobalt catalyst (4.72g) joined in the 1 liter of flask that contains deionized water (400ml) form slurry.

With H ₂PtCl ₆2H ₂O (0.282) and FeCl ₃6H ₂O (0.071g) is dissolved in and forms clear solution in the deionized water (80ml).Gradually iron and platinum solution are added in the slurry to (that is, with about 2ml/ minute speed) through 40 minutes times.The pH of slurry is maintained at about 4.0-4.4 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide solution with about 2ml in the interpolation process of platinum and ferrous solution adds in the slurry.

After solution added end of processing in the slurry to, this slurry stirred 30 minutes, and the pH of slurry is maintained at about 4.4.

This slurry is heated to 70 ℃ with about 2 ℃/minute speed then under nitrogen protection, its pH maintains 4.4 simultaneously.Reaching after 70 ℃, by add the pH that 0.1 weight % sodium hydroxide solution improves slurry according to following distribution mode: behind the 0.1 weight % sodium hydroxide solution that adds 1ml, pH was kept 10 minutes about 5.0, be increased to 5.5 and under this level, kept about 20 minutes by the 0.1 weight % sodium hydroxide solution that adds 2ml, stir about is 20 minutes then, reaches 6.0 constant pH in during this period of time.With NaBH ₄(0.38g) 12 weight % solution in deionized water (10ml) add in the slurry with 2ml/ minute speed.This slurry is heated to 70 ℃ then under nitrogen protection when stirring.

Behind precursor deposition, the catalyzer (5.0g) of platiniferous/iron joined in the tubular reactor described in the above embodiment 22 and in the hydrogen/argon atmospher described in the embodiment 36 handle.

This catalyzer contains the 2.5 weight % platinum of having an appointment, 0.3 weight % iron and 1 weight % cobalt.

Embodiment 38

This embodiment describes platinum and the deposition of cobalt on the catalyzer that contains 1 weight % cobalt that uses the acetonitrile preparation according to embodiment 27 described methods in detail.

The sample of 1 weight % cobalt catalyst (5.055g) joined in the 1 liter of flask that contains deionized water (400ml) form slurry.

With H ₂PtCl ₆2H ₂O (0.302) and CoCl ₂2H ₂O (0.044g) is dissolved in and forms clear solution in the deionized water (80ml).Gradually platinum solution is added in the slurry to (that is, with about 2ml/ minute speed) through 40 minutes times.The pH of slurry is maintained at about 3.5-4.0 by the common interpolation of 0.1 weight % sodium hydroxide solution.Sodium hydroxide that will about 2ml in the interpolation process of platinum solution joins in the slurry.

This slurry is heated to 70 ℃ with about 2 ℃/minute speed then under nitrogen protection, its pH maintains 4.4 simultaneously.Reaching after 70 ℃, by add the pH that 0.1 weight % sodium hydroxide solution improves slurry according to following distribution mode: behind the 0.1 weight % sodium hydroxide solution that adds 1ml, pH was kept 10 minutes about 5.0, be increased to 5.5 and under this level, kept about 20 minutes by the 0.1 weight % sodium hydroxide solution that adds 2ml, stir about is 20 minutes then, reaches 6.0 constant pH in during this period of time.This pH is increased to about 8.0 and be heated to 70 ℃ under nitrogen protection by the 0.1 weight % sodium hydroxide solution that adds 1ml then.

Behind precursor deposition, the catalyzer (5.0g) of platiniferous/cobalt joined in the tubular reactor described in the above embodiment 27 and in the hydrogen/argon atmospher described in the embodiment 36 handle.

This catalyzer contain have an appointment 2.5 weight % platinum and 1.3 weight % cobalts (from preparation procedure described in the above embodiment 27 1% and from the deposition program of describing in detail in the present embodiment 0.3%).

Embodiment 39

This embodiment describes the catalyzer for preparing in detail and is used in the PMIDA oxidising process under the condition that embodiment 24 describes in embodiment 36-38.

In embodiment 36 under 2.5% platinum of preparation, the PMIDA oxidizing condition that 1% cobalt catalyst is described in above embodiment 24 through testing 3 reaction times.

Under the PMIDA oxidizing condition that 2.5% platinum that also contains 0.3 weight % cobalt that makes in embodiment 38,1% cobalt catalyst are described in above embodiment 24 through testing 3 reaction times.

Under the PMIDA oxidizing condition in above embodiment 24, described of 2.5% platinum, 0.3% iron, 1% cobalt catalyst of preparation in embodiment 37 through testing 2 reaction times.

Test under the PMIDA oxidizing condition that 2.5% platinum, 0.3% iron, 1% cobalt catalyst of preparation are also described in above embodiment 24 in embodiment 37, in reaction time with bismuth oxide promotor (Bi ₂O ₃) (10mg) join in the reaction mixture.

Under the PMIDA oxidizing condition that 2.5% platinum, 0.3% iron, 1% cobalt catalyst of preparation are also described in above embodiment 24 in embodiment 37 through testing 4 reaction times, in 4 reaction times with bismuth oxide promotor (Bi ₂O ₃) (10mg) join in the reaction mixture.

The highest CO in exhaust ₂Ratio, the CO that in each reaction time, produces ₂The platinum lixiviate of total amount, the residual formaldehyde content in reaction, the formic acid content in reaction mixture and each test is summarised in the following table 21.

The reaction result of table 21 different catalysts

The performance of each is to similar with the catalyst mixture of test in embodiment 35 preparations in these catalyzer.The performance according to the platinum of people such as Ebner 6,417,133 preparation and iron catalyst of the period 1 performance of each in these catalyzer and test in above embodiment 35 is similar, although Shi Yan catalyzer only contains half platinum carrying capacity in the present embodiment.Yet, in the present embodiment Shi Yan catalyzer will be in down-stream in the stability of formaldehyde and formic acid oxidation with actively all fail on both.At last, according to the raising of formic acid content but it further is not oxidized to CO ₂, in the present embodiment Shi Yan catalyzer on performance, be similar to above described in the embodiment 28 and the test the catalyzer that contains 1% cobalt.In these catalyzer each demonstrates minimum platinum lixiviate, and it is inactive to prove that Pt becomes.

Bismuth promotor is introduced in some reaction time to determine whether that platinum is inactive at first or has not become inactive in subsequent cycle in fresh mixed catalyst.

When bismuth is introduced in the reaction mixture in first reaction time, according to formaldehyde and formic acid oxidation, catalyst performance equal at least above described in the embodiment 35 and test according to the platiniferous of people such as Ebner 6,417,133 preparation and the catalyzer of iron.This shows that Pt is active in first reaction time.

When bismuth when adding the 4th reaction time, catalyst performance is unaffected.With above in embodiment 28, describe and 1% cobalt catalyst of test similarly, the catalyzer of this platiniferous/iron comprises corresponding to bismuth promotor.This prompting Pt of initial activity in the catalyzer of platiniferous/iron will become inactive in follow-up reaction time.

Embodiment 40

Various carbon-supported cobalt carbide-nitride catalysts are generally to prepare by the atmosphere that change is incorporated in the reactor in the method described in the embodiment 27 according to above.

Methane/hydrogen environment: according to method described in the embodiment 27 in methane/hydrogen environment from contain the carbon-supported cobalt carbide-nitride catalyst of 1 weight % cobalt according to above precursor preparation in program described in the embodiment 26 preparation.The 100cm of 50%/50% (v/v) mixture by using methane and hydrogen ³/ minute air-flow in reactor, handle catalyst precursor (5.0g).

The ammonia reactor environment: according to method described in the embodiment 27 at NH ₃The carbon-supported cobalt carbide-nitride catalyst that contains 1 weight % cobalt in the environment from precursor preparation according to the preparation of program described in the above embodiment 26.By using 50cm ³/ minute NH ₃And 100cm ³/ minute the air-flow of argon gas in reactor, handle catalyst precursor (5.0g).

The ammonia reactor environment: according to method described in the embodiment 27 at NH ₃The carbon-supported cobalt carbide-nitride catalyst that contains 1 weight % cobalt in the environment from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 50cm ³/ minute NH ₃, 20cm ³/ minute hydrogen and 100cm ³The air-flow of/minute argon gas is handled in reactor.

Ammonia/methane reactor environment: according in method described in the embodiment 27 at NH ₃/ CH ₄The carbon-supported cobalt carbide-nitride catalyst that contains 1 weight % cobalt in the environment from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 25cm ³/ minute NH ₃, 25cm ³/ minute 50%/50% (v/v) mixture and 100cm of hydrogen/methane ³/ minute the air-flow of argon gas in reactor, handle.

Acetonitrile reaction device environment: the carbon-supported cobalt carbide-nitride catalyst that in containing the environment of acetonitrile, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 100cm ³/ minute argon gas and about 10cm ³/ minute the air-flow of acetonitrile steam in reactor, handle.

Butylamine environment: the carbon-supported cobalt carbide-nitride catalyst that in containing the environment of butylamine, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 100cm ³/ minute argon gas and about 15cm ³/ minute the air-flow of butylamine steam in reactor, handle.

Pyridine environment: the carbon-supported cobalt carbide-nitride catalyst that in containing the environment of pyridine, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 100cm ³/ minute argon gas and about 3cm ³/ minute the air-flow of pyridine steam in reactor, handle.

Pyrroles's environment: the carbon-supported cobalt carbide-nitride catalyst that in containing pyrroles's environment, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) is by using 100cm ³/ minute argon gas and about 2cm ³/ minute the air-flow of pyrroles's steam in reactor, handle.

Pyridine carbonitrile (picolonitrile) environment: the carbon-supported cobalt carbide-nitride catalyst that in containing the environment of pyridine carbonitrile, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) and pyridine carbonitrile (picolonitrile) are (3g) by using 100cm ³The air-flow of/minute argon gas is handled in reactor.

Melamine environment: the carbon-supported cobalt carbide-nitride catalyst that in containing the environment of melamine, contains 1 weight % cobalt according to method described in the embodiment 27 from precursor preparation according to the preparation of program described in the above embodiment 26.Catalyst precursor (5.0g) and melamine (1g) are by using 100cm ³The air-flow of/minute argon gas is handled in reactor.

Carbon-supported cobalt-containing catalyst prepares by using organometallic compound (cobalt (II) phthalocyanine).

To have about 1500m ²(Aldrich, Milwaukee WI) join in 1 liter of flask and form slurry for the particulate state carbon support (5.0g) of the Langmuir surface-area of/g and acetone (200ml).Cobalt (II) phthalocyanine (0.490g) is dissolved in is included in 1 liter of acetone (200ml) in the flask.Time through about 30-40 minute adds the solution that contains cobalt in the carbon support slurry to.

The mechanical stirring rod of use under 50% output rating stirred this slurry 48 hours under nitrogen protection under about 20 ℃.Slurry filters, then in vacuum drying oven at about 20cm ³/ minute little nitrogen gas stream in about 16 hours of 120 ℃ of dryings.The gained precursor contains the 1 weight % cobalt of having an appointment.

The catalyst precursor (5.0g) that drying is crossed joins in the haas troy C tubular reactor described in the embodiment 23.Reactor is in order to about 100cm ³/ minute the nitrogen introduced of speed purged about 15 minutes down at about 20 ℃.Thermopair is inserted into the reactor center of using for the precursor material charging.

The temperature of reactor is increased to about 950 ℃ through about 45 minutes time then in 100cc/ minute argon gas stream.The temperature of reactor kept about 120 minutes down at about 950 ℃.The gained catalyzer contains the 1 weight % cobalt of having an appointment.

Embodiment 41

This embodiment describes the PMIDA oxidation that every kind of catalyzer of various environment preparation carries out is adopted in use under condition described in the above embodiment 24 according to method described in the above embodiment 40 result in detail.The results are shown in the table 22.

Table 22 under different condition at the reaction result of 950 ℃ of following synthetic catalyzer

As shown in Table 22, and from CH ₃CN, butylamine, pyridine, pyrroles, pyridine carbonitrile, melamine and the catalyzer that the cobalt phthalocyanine makes are compared, from CH ₄/ H ₂, NH ₃, (NH ₃And H ₂) and (CH ₄/ H ₂And NH ₃) preparation catalyzer demonstrate than low activity.When reaction is driven to when being higher than the 80%PMIDA transformation efficiency, various cobalt catalyst demonstrate the oxidation of formaldehyde activity.

Embodiment 42

This embodiment describes the preparation method of the cobalt-containing catalyst with various metal carrying capacity and they in detail and is oxidized to use in the process of N-((phosphonomethyl)) glycine at PMIDA.

In these catalyzer each is by using the acetonitrile environment to synthesize according to program described in the above embodiment 40.In these catalyzer each is being tested in the PMIDA oxidation under the condition described in the embodiment 24 then.Each of PMIDA oxidation the results are shown in the following table 23.

Table 23 is by CH ₃CN handles the reaction result of synthetic CoCN/C

As shown in Table 23, all carbon-supported cobalt carbide-nitride catalyst demonstrates good PMIDA oxidation activity.Compare with carbon-supported ferrous-carbide-nitride catalyst, these catalyzer have also illustrated the active and much better stability of higher oxidation of formaldehyde.The carbon-supported cobalt carbide-nitride catalyst that contains 1-2 weight % cobalt demonstrates best total reaction characteristic.

Embodiment 43

This embodiment describes in detail from the method for the carbon-supported ferrous-carbide-nitride precursor of tetraphenylporphyrin (FeTPP) precursor preparation.

Carbon support (8.0g) joined in 1 liter of flask and add the acetone of 400ml and form slurry.To contain iron (III) tetraphenylporphyrin muriate (FeTPP) a kind of solution (200ml) (2.0g) in acetone was added drop-wise in the carbon slurry through 30-40 minute.Slurry at room temperature stirred 48 hours under nitrogen protection then.

The gained mixture filters, then in vacuum drying oven in little nitrogen gas stream 120 ℃ of one nights of drying.The gained precursor contains the 1.1 weight % iron of having an appointment.

Embodiment 44

This embodiment describes the catalyzer that allows according to the preparation of program described in above embodiment 23 and 43 in detail and experiences at the PMIDA oxidizing condition described in the embodiment 24.The results are shown in the table 24.

The reaction result of table 24 synthetic iron catalyst under varying environment

Whole carbon-supported ferrous-carbide-nitride catalysts suffer catalyst deactivation.The highest CO ₂Concentration and accumulation CO ₂With descending follow-up reaction time.Show high PMIDA oxidation activity from iron (III) tetraphenylporphyrin synthetic catalyzer, but produce a large amount of formaldehyde, aminomethylphosphonic acid and N-methyl-aminophosphonic acid, and demonstrate very little activity for the oxidation of formaldehyde and formic acid.From CH ₃CN synthetic catalyzer demonstrates PMIDA oxidation activity and oxidation of formaldehyde activity.

Embodiment 45

This embodiment describes in different carbonization environments preparation in detail and contains the method for catalyzer of molybdenum and tungsten and the use in the PMIDA oxidation of these catalyzer under condition described in the embodiment 24.

By using about 100cm ³/ minute air-flow replace at 50%/50% (v/v) of methane described in the embodiment 3 and hydrogen mixture, according to above in the method described in the embodiment 3 from contain the catalyzer of molybdenum and tungsten according to precursor preparation in the preparation of method described in the embodiment 2.

The catalyzer that contains 1 weight % molybdenum and 1 weight % tungsten according to the present embodiment preparation is tested under the PMIDA oxidizing condition described in the embodiment 24.According to also testing at the catalyzer that contains 10 weight % molybdenum carbides of the preparation of method described in the embodiment 3 with according to the catalyzer that contains 10 weight % tungsten nitride that method described in the embodiment 3 prepares under differing temps.

The results are shown in the table 25.

The reaction result of table 25 synthetic catalyzer under varying environment

With by CH ₄/ H ₂The catalyzer of Processing of Preparation is compared, and uses CH ₃CN handles prepared catalyzer and has more excellent PMIDA oxidation activity and oxidation of formaldehyde activity.

Embodiment 46

This embodiment describes the electroless copper on the 1 weight % cobalt catalyst that uses the acetonitrile preparation according to method described in the above embodiment 27 in detail.

1 weight % cobalt catalyst (15.5g) is joined in 1 liter of flask of the water (364ml) that contains purging with nitrogen gas and cross and form slurry.This flask is equipped with thermopair, nitrogen supply (NS) mouth and mechanical stirrer.

By copper sulfate (CuSO with reagent grade ₄5H ₂O) (20.65g) (Aldrich Chemical Co., Milwaukee, WI) and 91.2% tetrasodium ethylenediamine tetraacetate (EDTANa4) (41.82g) add in the water (950ml) that purging with nitrogen gas crosses and prepare copper plating solution.Mixture is cooled in about 10 ℃ and the slurry that coating solution is added to contain catalyzer.Prepare the solution of 37 weight % formalin (20.13) in the water (305ml) that purging with nitrogen gas is crossed, be added drop-wise in the plating mixture through 90 minutes time then.

The pH of coating solution monitors by use pH meter in the interpolation process of the solution that contains formalin.In 90 minutes interpolation times of the solution that contains formalin, the pH of plating mixture changes to 13.4 (at 10.8 ℃) from 13.65 (at 9.4 ℃), changes to 13.2 (at 11.7 ℃) at last.Plating mixture stir about 30 minutes.

The sedimentation from the plating mixture of the catalyzer of plating is reclaimed catalyzer by filtering from mixture in nitrogen atmosphere.Filtrate (1533g) is reclaimed from mixture.Gained wet cake in the vacuum that nitrogen purging is crossed dry about 8 hours.The weighing of exsiccant catalyzer is about 20.21 grams, and inductively coupled plasma (ICP) analysis has obtained the copper content of about 22.5 weight %.

Embodiment 47

This embodiment describes the dehydrogenation that is used for diethanolamine according to the copper containing catalyst of the preparation of method described in the embodiment 46 in detail.

This reactor earlier with argon cleaning (when on technical scale, carrying out this reaction, N ₂Be preferred).Mixture contains sodium hydroxide (99.81g) (Aldrich Chemical Co., Milwaukee, WI) 50 weight % solution, diethanolamine (62.50g) (Huntsman Chemicals), 22.5% bronze medal/1% cobalt catalyst (making according to method described in the embodiment 46) (12.4g) and deionized water (75ml) are produced the total reaction mixtures of 250 grams.Reactor is with nitrogen purging and with nitrogen supercharging to 135 pound/square inch.Reaction mixture then when stirring the process through 2 hours be heated to 150 ℃.Based on the amount of the hydrogen that produces in reaction process, the transformation efficiency from the diethanolamine to the Iminodiacetic acid sodium salt is about 1%.

Embodiment 48

Various carbon-supported catalyzer that contain transition metal and their carrier analysis are measured their Langmuir surface-area.The catalyzer and the carrier of test comprise: the above carbon support of describing in embodiment 22, according to the 1%FeCN/C catalyzer of embodiment 23 preparations, the 1%CoCN/C catalyzer according to embodiment 27 preparations has about 1600m ²The carbon support of the surface-area of/g and the 1%FeTPP/C catalyzer for preparing according to people International Publication No.WO 03/068387A1 such as Coleman.Measure whole surface-area, belong to the surface-area of the hole (that is micropore) that diameter is lower than 20 dusts and belong to the surface-area of diameter greater than the hole (that is, mesoporosity and macrovoid) of 20 dusts.What surface-area was measured the results are shown in the table 26.

Table 26

Figure 17 has shown the contrast of the pore surface area of 1%Fe, 1%Co catalyzer and carbon support.Figure 18 has compared the pore surface area of 1.1%FeTPP catalyzer and its carbon support.As shown in Figure 17, the 1%Fe catalyzer has about 80% the surface-area that is equivalent to its carbon support total surface area, and the 1%Co catalyzer has about 72% the surface-area that is equivalent to the support of the catalyst total surface area.As shown in Figure 18, the 1.1%FeTPP catalyzer has about 55% the surface-area that is equivalent to its carbon support total surface area.

Embodiment 49

Analyze nitrogen and levels of transition metals according to the 1%CoCN/C of method described in the embodiment 28 preparation and 1.5%CoCN/C catalyzer by inductively coupled plasma (ICP) analytical method to measure them.The results are shown in the table 27.

Table 27

Embodiment 50

This embodiment describes the X-ray powder diffraction of the various catalyzer that prepare in detail and analyzes (XRD) under different condition.These catalyzer generally prepare according to above embodiment 23,27,40 or 43 described programs.Sample and their condition of preparation are described in the following table 28.

Table 28

Catalyst sample	Processing conditions
		1)1.5％CoCN/C	At 950 ℃ of following CH ₃CN handled 2 hours
2)5％CoCN/C	At 950 ℃ of following CH ₃CN handled 2 hours
		3)5％CoCN/C	At 950 ℃ of following CH ₃CN handled 4 hours
4)10％CoCN/C	At 950 ℃ of following CH ₃CN handled 2 hours
		5) embodiment 22 carriers	At 950 ℃ of following CH ₃CN handled 2 hours
6) 1%Co-phthalocyanine (PLCN) CN/C	Handled 2 hours at 950 ℃ of following argon gas
		7)1.1％FeTPP/C	Handled 2 hours at 800 ℃ of following argon gas
8)1％FeCN/C	At 950 ℃ of following CH ₃CN handled 2 hours

Powdered sample is by they directly being positioned in the zero background reservoir, then they is directly put into the Cu radiation of adopting 40KV/30mA and is equipped with in the Philips PW1800 Θ/Θ diffractometer of diffracted beam monochromator to remove fluorescent radiation analysis from cobalt.

The diffractogram of sample 1-8 is shown in respectively among Figure 19-26.The diffractogram of sample 1-4 and 6 (Figure 19-22 and 24) detects face-centered cubic (FCC) form of graphite and cobalt.Sreen analysis mutually is to be undertaken by the diffracted ray of broadening for the particle sensitivity in 100-2000 dust scope to cobalt with graphite.The result is summarised in the following table 29.

Table 29

The diffractogram of sample 7 (Figure 25) detects graphite and iron carbide (Fe ₃C).Sreen analysis provides＞granularity of the graphite of 1000 dusts and about 505 dusts.The diffractogram of sample 8 (Figure 26) detects graphite, chromium nitride (CrN), nitrided iron (FeN), chromium and iron carbide (Fe ₃C).Sreen analysis obtains the graphite particle size of about 124 dusts, the chromium nitride granularity of about 183 dusts and the nitrided iron granularity of about 210 dusts.

Sample

1 and 2 is carried out quantitative analysis.Preferred internal standard is ZnO, because it has fully been characterized and do not had the line at overlapping required peak.The sample 1 of about 100mg and 2 mixes with 10.7%ZnO (sample 1) and 4.89%ZnO (sample 2), uses above-described XRD program to test then.The diffraction of

sample

1 and 2 pattern is provided in respectively in Figure 27 and 28.

Use Rivetfeld revised law (refinement) that

sample

1 and 2 is carried out quantitative analysis then, to measure the amount of each phase.It is whole pattern-fitting program that Rivetfeld revises, and it with it and the contrast of experiment pattern, calculates the error between two patterns with the first principles computations diffraction pattern, revises theoretical pattern then till residual errors minimizes.In both cases, Rivetfeld revises the loq residual errors that has obtained in the 5-7% scope.The Rivetfeld correction result is listed in the following table 30.

Table 30

The estimation of

sample

3 and 6 weight fraction is provided in the table 31.

Table 31

Figure 29 and 30 provides

sample

2 and 3 and the contrast of the diffractogram of

sample

3 and 6 respectively.

Embodiment 51

This embodiment describes the scanning electron microscopy (SEM) and the transmission electron microscopy (TEM) of the

sample

1,2,4,7 described in the above embodiment 50 and 8 in detail and analyzes.Sem analysis is undertaken by use the JEOL JSM 6460LV scanning electronic microscope of operating under 30kV.TEM characterize to be to carry out at the JEOL 1200 EX TEM that operate under 120 keV and/or the JEOL 2000 EX TEM that operate under 200 keV by using.

Figure 31 and 32 has shown the view of powder of sample 1 and the SEM image of viewgraph of cross-section.Figure 33 and 34 has shown the distribution of carbon nanotube on carbon base material surface and the SEM image of the form of carbon nanotube.Figure 35 and 36 is the SEM images of carbon nanotube that shown the powdered sample of sample 1.

Figure 37 and 38 has shown the view of powder of sample 2 and the SEM image of viewgraph of cross-section.Figure 39 and 40 has shown the distribution of cobalt granule on the powdered sample of sample 2 and the SEM image of viewgraph of cross-section.Figure 41 has shown the image at the SEM of the lip-deep carbon nanotube of carbon support.Figure 42 is the energy-dispersive X-ray analysis spectrum (EDS) of the powdered sample of sample 2.The EDS spectrum of sample 2 is by using Oxford energy dispersive X ray spectroscopy system to measure.

Figure 43 and 44 is respectively the TEM image of sample 4 under low and high x magnification.

Figure 45 is the SEM image of the powdered sample of sample 7.Figure 46 is the backscattered electron image of the powdered sample of sample 7.

Figure 47 and 48 is TEM images of the cross-sectional view of show sample 7.

Figure 49 is the SEM image of the powdered sample of sample 8.Figure 50 is the backscattered electron image of the powdered sample of sample 8.Figure 51 and 52 is that the high power of powdered sample 8 is amplified the SEM image, has shown the growth of carbon nanotube on carbon support.Figure 53 and 54 provides the TEM image of the viewgraph of cross-section of sample 8.

Embodiment 52

This embodiment describes the X-ray photoelectron spectroscopy analysis (XPS) (listing in detail) of the sample of describing among the above embodiment 50 in detail in table 28.

XPS analysis is to carry out under the analysis condition of listing in table 32.

Table 32

Instrument	Physical?Electronics?Quantum?2000?Scanning?XPS
		X-ray source	Monochromatic?Al?Kα
Analyze area	0.4mm?x?0.4mm
		Exit angle
	45 degree
		Electric charge is proofreaied and correct	C-C in being set in the Cls spectrum of 284.8eV, C-H
Charge neutralization	Low-energy electron and ion overflow

Surface concn result's (area evaluation) by the sample 1-6 of atom % and weight % describes in detail in the table 33 and 34 respectively below.

Table 33

Sample	C	N	O	Cl	Co
							1	97.3	1.2	1.0	0.07	0.42
2	97.9	0.2	1.3	0.09	0.52
						3	97.9	0.7	0.9	0.05	0.41
4	97.7	0.4	1.2	0.08	0.73
						5	97.3	1.8	0.8	0.07	-
6	98.5	0.4	0.8	0.10	0.19

Table 34

Sample	C	N	O	Cl	Co
							1	95.1	1.4	1.3	0.2	2.0
2	95.4	0.3	1.6	0.3	2.5
						3	95.9	0.8	1.2	0.1	2.0
4	94.4	0.4	1.5	0.2	3.5
						5	96.6	2.1	1.1	0.2	-
6	97.3	0.5	1.0	0.3	0.9

Sample 1-4 and 6 cobalt 2p3 curve-fitting results are summarised in the following table 35.

Table 35

Sample	%Co presses metal	%Co is as oxide compound
			1	27	73
2	47	53
			3	35	65
4	35	65
			6	61	39

Surface concn result's (area evaluation) by the sample 7-8 of atom % and weight % lists in the table 36 and 37 respectively below in detail.

Table 36

Sample	C	N	O	Na	Cl	Fe
							7	97.6	0.7	1.5	0.0	0.1	0.2
8	95.2	0.6	2.6	0.7	0.2	0.8

Table 37

Sample	C	N	O	Na	Cl	Fe
							7	96.2	0.7	2.0	0.0	0.3	0.7
8	90.8	0.6	3.3	1.3	0.6	3.3

The iron curve-fitting results of sample 7-8 (Fe of %) is summarised in the following table 38.

Table 38

Sample	%Fe presses metal	%Fe is by oxide/hydroxide
			7	7	93
8	43	57

Figure 54 is the XPS spectrum of sample 1-6.

Figure 55 has shown the XPS spectrum of sample 7 and 8.

＊＊＊＊＊＊＊＊

The present invention is not limited to above embodiment and can in addition different improvement.The narration of above preferred embodiment (comprising embodiment) is only used for making technician of the prior art to understand the present invention, its principle and their practical application, so that those skilled in the art can adapt to and employing the present invention with a lot of forms, also can be very suitable for the requirement of concrete purposes.

" comprise " or the use of " comprising " for the word that in whole specification sheets, (comprises claims), unless this paper needs in addition, otherwise these words be according to following basis and clear understand use: they are to comprise but not exclusively explain, and the applicant wishes that each these word is all so explained when understanding whole specification sheets.

Claims

1. the method for oxidation N-((phosphonomethyl)) iminodiethanoic acid or its salt; this method comprises allows N-((phosphonomethyl)) iminodiethanoic acid or its salt and oxygenant contact containing transition metal and do not contain substantially in the presence of the noble metal active oxide catalyst mutually, and the wherein said oxide catalyst that contains transition metal comprises:

Formed thereon the transition metal composition that contains transition metal and nitrogen carbon support and

At the lip-deep carbon nanotube of carbon support.

2. method according to claim 1, wherein said transition metal composition contain and are selected from following transition metal: copper, silver, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium, cerium and their mixture.

3. method according to claim 2, wherein said transition metal are selected from chromium, iron, cobalt and their mixture.

4. method according to claim 3, wherein said transition metal comprises iron.

5. method according to claim 3, wherein said transition metal comprises cobalt.

6. method according to claim 1, wherein said transition metal composition contain transition metal nitride, transition metal carbide-nitride or their mixture.

7. method according to claim 6, wherein said transition metal composition contains transition metal nitride.

8. method according to claim 1, the wherein said oxide catalyst that contains transition metal comprises the particulate state carbon support.

9. method according to claim 1, wherein said carbon nanotube comprise a part of transition metal of described transition metal composition.

10. method according to claim 1, wherein said carbon nanotube comprise a part of nitrogen of described transition metal composition.

11. according to each described method among the claim 1-10, the wherein said transition metal composition that on carbon support, forms account for the described oxide catalyst that contains transition metal at least about 0.1 weight %.

12. method according to claim 11, the wherein said transition metal composition that forms on carbon support account for the described about 0.1-20 weight % that contains the oxide catalyst of transition metal.

13. according to each described method among the claim 1-10, the transition metal in the wherein said transition metal composition that on carbon support, forms account for the described oxide catalyst that contains transition metal at least about 0.1 weight %.

14. method according to claim 13, the transition metal in the wherein said transition metal composition that forms on carbon support account for the described about 0.1-20 weight % that contains the oxide catalyst of transition metal.

15. according to each described method among the claim 1-10, the nitrogen in the wherein said transition metal composition that on carbon support, forms account for the described oxide catalyst that contains transition metal at least about 0.1 weight %.

16. method according to claim 15, the nitrogen in the wherein said transition metal composition that forms on carbon support account for the described about 0.1-5 weight % that contains the oxide catalyst of transition metal.

17. according to each described method among the claim 1-10, wherein said transition metal composition on carbon support comprises discrete particle.

18. method according to claim 17, wherein said transition metal composition particulate has the granularity that is lower than about 1000nm at least about 95 weight %, by their overall dimension.

19. method according to claim 17, wherein said transition metal composition particulate has the granularity that is lower than about 250nm at least about 80 weight %, by their overall dimension.

20. method according to claim 17, wherein said transition metal composition particulate has the granularity that is lower than about 18nm at least about 60 weight %, by their overall dimension.

21. method according to claim 17, wherein said transition metal composition particulate has the granularity that is lower than about 1nm at least about 20 weight %, by their overall dimension.

22. method according to claim 21, the about 20-95 weight of wherein said transition metal composition particulate % has the granularity that is lower than about 1nm, by their overall dimension.

23. according to any one described method among the claim 1-10, wherein total Langmuir surface-area of carbon support is at least about 1000m before forming transition metal composition on the carbon support ²/ g.

24. method according to claim 23, wherein total Langmuir surface-area of carbon support is about 1000-1600m before forming transition metal composition on the carbon support ²/ g.

25. according to any one described method among the claim 1-10, the wherein said total Langmuir surface-area that contains the oxide catalyst of transition metal is at least about 1000m ²/ g, and be carbon support before forming transition metal composition on the carbon support total Langmuir surface-area at least about 60%.

26. according to the method for claim 25, the wherein said total Langmuir surface-area that contains the oxide catalyst of transition metal is about 1000-1400m ²/ g, and be about 60-80% of total Langmuir surface-area of carbon support before forming transition metal composition on the carbon support.

27. according to any one described method among the claim 1-10, the wherein said micropore Langmuir surface-area that contains the oxide catalyst of transition metal is about 750-1100m ²/ g.

28. according to any one described method among the claim 1-10, the wherein said micropore Langmuir surface-area that contains the oxide catalyst of transition metal is about 55-80% of the micropore Langmuir surface-area of carbon support before forming transition metal composition on the carbon support.

29. according to any one described method among the claim 1-10, the wherein said total Langmuir surface-area that contains the oxide catalyst of transition metal is at least about 1200m ²/ g, and the described micropore Langmuir surface-area that contains the oxide catalyst of transition metal is about 750-1100m ²/ g.

30. according to any one described method among the claim 1-10, the wherein said total Langmuir surface-area that contains the oxide catalyst of transition metal is at least about 1200m ²/ g, and described total mesopore and the macropore Langmuir surface-area that contains the oxide catalyst of transition metal is about 175-300m ²/ g.

31. according to any one described method among the claim 1-10; wherein said N-((phosphonomethyl)) iminodiethanoic acid or its salt contact with oxygenant in the presence of catalyst system, and wherein catalyst system comprises the described catalyzer that contains the oxide catalyst of transition metal and contain precious metal.

32. according to any one described method among the claim 1-10, the wherein said oxide catalyst that contains transition metal is effective for the oxidation of the by product formaldehyde that produces in the oxidation of N-((phosphonomethyl)) iminodiethanoic acid or its salt.

33. method according to claim 32, the wherein said oxide catalyst that contains transition metal is effective for the oxidation of the by product formic acid that produces in the oxidation of N-((phosphonomethyl)) iminodiethanoic acid or its salt.